Classifications

• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C231/00—Preparation of carboxylic acid amides
  • C07C231/02—Preparation of carboxylic acid amides from carboxylic acids or from esters, anhydrides, or halides thereof by reaction with ammonia or amines

Definitions

• the present invention relates to a process for preparing N,N-dimethylacetamide (DMAC) by continuously reacting methyl acetate (MeOAc) with dimethylamine (DMA) in the presence of a basic catalyst.
• DMAC N,N-dimethylacetamide
• DMAC finds use as a polar solvent, for example for polymers and for gases, as paint removers, extractants, catalysts and crystallization assistants.
• DMAC is used, owing to its high boiling point, for specific coating materials based on polymeric binders, for example polyamides and polyurethanes.
• DMAC is also used for producing fibers and films and as a reaction medium. In the spinning of Spandex® fibers, DMAC is used as an assistant and subsequently recovered at least partly.
• DMAC may be prepared from acetic acid and dimethylamine, for example according to FR-A-1,406,279.
• Carboxamides are also obtainable by aminolysis of corresponding carboxylic esters; cf., for example, ‘Organikum’, VEB Deutscher Verlag dermaschineen, 1963, pages 374-375.
• CA-A-1 073 467 and CA-A-1 073 468 (both General Electric Comp.) describe the preparation of diols and N,N-dialkylamides by reacting carboxylic diol esters with dialkylamines.
• Example 1 a “20% methanol-methyl acetate azeotrope” is used for the reaction at 155-160° F. (68.4-71.2° C.).
• JP-A-02 160749 (Lion Akzo KK) relates, according to the Patent Abstracts of Japan, to the reaction of aliphatic carboxylic esters with ammonia or an amine, such as monomethylamine, ethylenediamine, diethylenetriamine, in the presence of an “alkali catalyst” at from 50 to 180° C., in particular from 80 to 160° C., and in the pressure range from standard pressure to 9.81 bar (10 kg ⁇ cm ⁇ 2 ⁇ G). From 0.1 to 10 mol %, in particular from 1 to 5 mol %, based on the carboxylic ester used, of sodium methoxide (NaOMe) is used as the catalyst.
• NaOMe sodium methoxide
• German patent applications No. 102004030616.8 of 24 Jun. 2004 and DE-A-1 0 315 214 to BASF AG relate to processes for purifying DMAC.
• the process should afford DMAC in high yield and space-time yield and in high purity (for example free or virtually free of acetic acid, high color quality).
• a process has been found for preparing N,N-dimethylacetamide (DMAC) by continuously reacting methyl acetate (MeOAc) with dimethylamine (DMA) in the presence of a basic catalyst, which comprises using MeOAc in the form of a methanolic solution which is obtained as a by-product in the preparation of polyTHF by transesterifying polyTHF diacetate with methanol.
• MeOAc methyl acetate
• DMA dimethylamine
• DMAC dimethylamine
• MeOAc methyl acetate
• DMA dimethylamine
• the DMA used preferably has a purity of ⁇ 99% by weight, in particular ⁇ 99.4% by weight, and is, for example, in the range from 99.5 to 99.8% by weight.
• the methanolic MeOAc solution preferably has a concentration in the range from 65 to 90% by weight, preferably from 70 to 85% by weight, in particular from 75 to 82% by weight, of MeOAc.
• the methanolic MeOAc solution used is a corresponding by-product stream which is obtained in the production of polyTHF (polytetrahydrofuran), for example by the two-stage BASF process according to EP-A-3112, DE-A-197 58 296 and/or DE-A-198 17 113.
• polyTHF polytetrahydrofuran
• the methanolic MeOAc solution preferably has the following contents:
• the methanolic MeOAc solution consists of MeOAc, MeOH, dimethyl ether, THF and water in the above-specified amounts.
• the continuous reaction is preferably carried out at an absolute pressure in the range from 1 to 200 bar, preferably from 3 to 100 bar, in particular from 10 to 30 bar, very particularly from 12 to 25 bar, for example from 15 to 20 bar.
• the reaction temperature is preferably in the range from 20 to 200° C., preferably from 60 to 140° C., in particular from 80 to 120° C., very particularly from 90 to 110° C., for example from 95 to 105° C.
• Useful reactors for the inventive reaction are in particular backmixed reactors, for example stirred tank reactors or jet loop reactors, nonbackmixed reactors such as stirred tank batteries or tubular reactors, and special designs such as reaction columns with and without internal or external delay volumes, in which internal and external heat removal is possible.
• the reaction is effected with particular preference in a jet loop reactor.
• the jet loop reactor is preferably equipped with an insert tube and nozzle at the bottom. Preference is given to adding DMA together with the catalyst through the circulation-pumped driving jet and the MeOAc through the outer jet.
• a postreactor for example a flow tube or a cascaded delay vessel.
• the basic catalyst used is preferably an alkali metal hydroxide, alkaline earth metal hydroxide, alkali metal alkoxide, alkaline earth metal alkoxide, alkali metal carbonate, alkaline earth metal carbonate, alkali metal hydrogencarbonate, alkaline earth metal hydrogencarbonate and/or an amine, in particular tertiary amine.
• the alkali metal is Li, Na, K, Rb or Cs, in particular Na or K.
• the alkaline earth metal is Be, Mg, Ca, Sr or Ba, in particular Mg or Ca.
• the alkoxide is preferably a C 1-4 -alkoxide, in particular methoxide.
• the amine is preferably a C 3-12 -alkylamine, for example triethylamine, tri-n-propylamine, tri-n-butylamine, dimethylethylamine, diethylmethylamine, N-methylpiperidine, triethylenediamine (TEDA).
• TAA triethylenediamine
• a very particularly preferred catalyst in the process according to the invention is sodium methoxide (NaOMe).
• the catalyst is present in the reaction mixture in homogeneous and/or suspended form.
• the catalyst or the catalyst mixture is advantageously used in the form of a solution and/or suspension in a solvent or suspension medium.
• Preferred solvents and/or suspension media are water and alcohols (e.g. C 1-4 -alcohols such as methanol, ethanol, n-propanol, n-butanol) or mixtures thereof.
• alcohols e.g. C 1-4 -alcohols such as methanol, ethanol, n-propanol, n-butanol
• the catalyst or the catalyst mixture is used in the abovementioned preferred amounts, preferably in the form of from 1 to 35% by weight, in particular from 5 to 30% by weight, solution or suspension.
• the catalyst used is NaOMe in the above-mentioned preferred amounts in the form of a methanolic solution, in particular in the form of a from 1 to 35% by weight solution, very particularly in the form of a from 25 to 30% by weight solution.
• the reaction of the MeOAc in the process according to the invention is preferably carried out in the presence of less than 1% by weight, particularly less than 0.5% by weight, very particularly in the range from 0 to 0.3% by weight, of water, based in each case on the weight of the two feedstocks, MeOAc and DMA (in total).
• the heat of reaction is removed preferably via an external heat exchanger.
• the steam raised in the external heat exchanger for example 1.5 bar steam, is utilized in a synthesis plant for methylamines from methanol and ammonia.
• the liquid reactor effluent from the synthesis stage consists of
• tetrahydrofuran (THF) and/or dimethyl ether may be such by-products.
• liquid reactor effluent may be decompressed directly into a boiler of a distillation column.
• decompression is effected into two alternately operated distillation boilers.
• water or an aqueous or anhydrous protic acid such as sulfuric acid, methanesulfonic acid, carboxylic acid (e.g. C 1-4 -carboxylic acid), in particular phosphoric acid, is added to the effluent, preferably in an amount which ensures full conversion of the basic catalyst used to the corresponding acid and to the corresponding alkali metal, alkaline earth metal or ammonium salt of the protic acid.
• protic acid such as sulfuric acid, methanesulfonic acid, carboxylic acid (e.g. C 1-4 -carboxylic acid), in particular phosphoric acid
• the organic product mixture is preferably removed from salts present by evaporation (at standard pressure or under reduced pressure, for example in a reboiler), for example until a salt which precipitates out distinctly reduces the heat exchanger output and leads to encrustations.
• the boiler for the reactor effluent is then preferably changed and the residue of the old boiler is concentrated as far as possible by evaporation.
• the precipitated solid salt residue may be dissolved in water and disposed of as a solution in a water treatment plant.
• the reactor effluent which has been evaporated off from the solid and partially or totally condensed is worked up by distillation, for example in one, two, three, four or more columns which are connected to one another if appropriate.
• methanol and any other low boilers are removed overhead at preferably from 0.8 to 1.2 bar.
• an aqueous or anhydrous methanol stream which may comprise DMA is enriched and is, for example, advantageously recycled for use in a methylamine synthesis plant (in particular for DMA preparation).
• the bottom effluent of column A is fed to a column B.
• pure DMAC ⁇ 99.5% by weight, in particular ⁇ 99.7% by weight, very particularly ⁇ 99.8% by weight, for example in the range from ⁇ 99.9 to 99.99% by weight
• a liquid side draw which is disposed preferably in the rectifying section.
• the top effluent of column B comprising DMAC (e.g. ⁇ 98% by weight of DMAC, in particular from 98.5 to 99.5% by weight of DMAC), is preferably recycled into column A.
• DMAC e.g. ⁇ 98% by weight of DMAC, in particular from 98.5 to 99.5% by weight of DMAC
• the bottom effluent of column B is separated once more in a column C, preferably at standard pressure, and the top effluent comprising DMAC and methanol (e.g. approx. 94% by weight of DMAC and approx. 6% by weight of methanol) is preferably likewise recycled to column A and the bottom effluent of column C (high boilers, DMAC and added methanol) passes to disposal, for example incineration.
• the third column C distinctly reduces the amount of residue.
• the distillative purification of DMAC may also be effected according to one of the processes of the two German patent applications 102004030616.8 of Jun. 24, 2004 and DE-A-10 315 214 (both BASF AG).
• the process may advantageously also be carried out in a plant which has originally been designed for the preparation of N,N-dimethylformamide (DMF) from carbon monoxide (CO) and DMA.
• DMF N,N-dimethylformamide
• Slight modifications/plant improvements thus advantageously allows both DMF and DMAC, for example in alternating operation, to be prepared in the DMF plant as described, for example, in K. Weissermel, H.-J. Arpe, Industrielle Organische Chemie, Wiley-VCH, 5th edition 1998, page 49, or in general and in principle in JP-A2-110 92 434.
• the invention also enables the alternative or alternating production of DMAC in a DMF plant.
• DMAC yields in the range of ⁇ 88%, in particular ⁇ 95%, very particularly ⁇ 99%, for example from 99.5 to 99.9% (based in each case on MeOAc used), at MeOAc conversions in the range of ⁇ 90%, in particular ⁇ 96%, very particularly ⁇ 99%, for example from 99.5 to 100%.
• the DMAC space-time yields are in the range from 0.1 to 0.85 kg of DMAC/(liter of reactor volume ⁇ h), for example from 0.2 to 0.5 kg of DMAC/(liter of reactor volume ⁇ h).
• the process according to the invention affords DMAC with a purity of ⁇ 99.5% by weight, in particular ⁇ 99.7% by weight, very particularly ⁇ 99.8% by weight, for example in the range from ⁇ 99.9 to 99.99% by weight (see below for method and conditions for purity determination),
• a water content ⁇ 200 ppm for example in the range from 50 to 150 ppm (to DIN 51777), and
• the acid content (calculated as acetic acid) of the DMAC is in particular ⁇ 80 ppm, very particularly ⁇ 70 ppm, for example in the range from 5 to 60 ppm (to DIN 53402).
• DMA dimethylamine
• methanolic methyl acetate 77.5% by weight
• the water content in the feed (DMA+methanolic methyl acetate) was 109 ppm.
• the reaction was effected in a loop reactor with a mean residence time (MRT) of 1 h and sodium methoxide (0.48 g/h) in methanolic solution (30% by weight) as the homogeneous catalyst.
• MRT mean residence time
• the heat was removed via an external heat exchanger. The energy removed in the external heat exchanger can raise 1.5 bar steam.
• the liquid effluent from the synthesis stage consisted of 57.7% by weight of DMAC, 34.2% by weight of methanol, 5.0% by weight of methyl acetate and a total of 3.1% by weight of DMA, tetrahydrofuran, sodium methoxide and by-products.
• Example 2 All settings from Example 1 were adopted. However, the water content of the feed stream was 550 ppm. After a short time, there were blockages in the reactor as a result of precipitated sodium acetate, and the experiment had to be stopped.
• the reaction was effected in a loop reactor with a mean MRT of 1 h and sodium methoxide (0.56 g/h) in methanolic solution (30% by weight) as the homogeneous catalyst.
• the heat was removed via an external heat exchanger. The energy removed in the external heat exchanger can generate 1.5 bar steam.
• the liquid effluent from the synthesis stage consisted of 53.9% by weight of DMAC, 36.3% by weight of methanol, 3.9% by weight of methyl acetate and a total of 5.9% by weight of DMA, tetrahydrofuran, sodium methoxide and by-products.
• This effluent was conveyed in straight pass through a tubular reactor at 120° C., 20 bar and a mean MRT of 1 h.
• the effluent consisted of 58.3% by weight of DMAC, 37.3% by weight of methanol, 1.1% by weight of methyl acetate and a total of 3.3% by weight of DMA, tetrahydrofuran, sodium methoxide and by-products.
• a reaction effluent according to Example 3 was admixed continuously with 85% phosphoric acid for the stoichiometric formation of Na 2 HPO 4 .
• 400 g/h of the condensed mixture were fed continuously to a distillation column, and a high boiler stream (218 g/h) comprising 99.2% by weight of DMAC and 0.8% by weight of by-products was drawn off at a bottom temperature of 175° C.
• this stream was worked up further, and 198 g/h of DMAC with a purity of 99.9% were obtained from a side draw.

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• 2004
  • 2004-12-06 DE DE102004058886A patent/DE102004058886A1/de not_active Withdrawn
• 2005
  • 2005-12-03 US US11/720,774 patent/US20080207949A1/en not_active Abandoned
  • 2005-12-03 CN CN2005800418295A patent/CN101072748B/zh not_active Expired - Fee Related
  • 2005-12-03 WO PCT/EP2005/012982 patent/WO2006061159A1/de not_active Ceased
  • 2005-12-03 EP EP05815808.0A patent/EP1828102B1/de not_active Expired - Lifetime
  • 2005-12-03 ES ES05815808.0T patent/ES2472271T3/es not_active Expired - Lifetime
  • 2005-12-03 JP JP2007544789A patent/JP5080268B2/ja not_active Expired - Fee Related
• 2010
  • 2010-12-14 US US12/967,798 patent/US8338644B2/en not_active Expired - Fee Related

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