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US20090223805A1 - Process for preparing n,n-dimethylaminoethoxyethanol - Google Patents

Process for preparing n,n-dimethylaminoethoxyethanol Download PDF

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Publication number
US20090223805A1
US20090223805A1 US12/293,699 US29369907A US2009223805A1 US 20090223805 A1 US20090223805 A1 US 20090223805A1 US 29369907 A US29369907 A US 29369907A US 2009223805 A1 US2009223805 A1 US 2009223805A1
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distillation
dimethylaminoethoxyethanol
process according
bottom fraction
distilling
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US12/293,699
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Frank-Friedrich Pape
Alfred Krause
Johann-Peter Melder
Bernd Stein
Joachim-Thierry Anders
Frank Haese
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BASF SE
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BASF SE
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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C213/00—Preparation of compounds containing amino and hydroxy, amino and etherified hydroxy or amino and esterified hydroxy groups bound to the same carbon skeleton
    • C07C213/04—Preparation of compounds containing amino and hydroxy, amino and etherified hydroxy or amino and esterified hydroxy groups bound to the same carbon skeleton by reaction of ammonia or amines with olefin oxides or halohydrins
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00002—Chemical plants
    • B01J2219/00004—Scale aspects
    • B01J2219/00006—Large-scale industrial plants

Definitions

  • the invention relates to a process for preparing N,N-dimethylaminoethoxyethanol, to an apparatus for performing it and to the use of by-products of the preparation of N,N-dimethylaminoethanol in such a process.
  • 2-[2-(dimethylamino)ethoxy]ethanol (N,N-dimethylaminoethoxyethanol, DMAEE) is a commercially available compound (BASF Corporation, USA), which finds use, for example, as an intermediate in the synthesis of active pharmaceutical ingredients or a catalyst in polyurethane preparation.
  • DMAEE is prepared firstly by reacting diethylene glycol with dimethylamine over a catalyst (see, for example, EP-A 0 303 323, JP-A 62/051646, JP-A 08/143,520 and JP-A 09/020,735), and secondly by reacting N,N-dimethylethanolamine with ethylene oxide (see, for example, J. G. Cannon et al., Journal of Pharmaceutical Sciences 62 (1973) 830 and U.S. Pat. No. 3,853,818).
  • DMAEE forms in industrially utilizable amounts in the industrial preparation of N,N-dimethylethanolamine and can be removed in a simple manner in the purification of the N,N-dimethylethanolamine.
  • the invention therefore provides a process for preparing N,N-dimethylaminoethoxyethanol (DMAEE), wherein
  • the invention further provides for the use of the bottom stream of a distillation of the reaction mixture of dimethylamine and ethylene oxide for obtaining DMAEE.
  • the invention likewise provides an apparatus for performing the above-described process, comprising (I) a reactor, preferably a tubular reactor, with inlets for dimethylamine and ethylene oxide and an outlet for the reaction product, (II) a distillation apparatus for enriching the DMAEE by distillatively removing N,N-dimethylethanolamine from the reaction mixture with an outlet for the DMAEE-containing bottom product at the bottom of the distillation apparatus and (III) an apparatus which is suitable for fractional distillation and has an inlet for the DMAEE-containing reaction mixture at the bottom or at the side and an outlet for the distilled DMAEE in the top region of the apparatus.
  • the process according to the invention can provide DMAEE in a simple manner and without complicated synthesis with catalysts and complex product mixtures. It is also advantageous that, to obtain a color-stable pure material, hydrogenation over a noble metal catalyst is not necessary.
  • the reaction mixture formed comprises generally from 1 to 6% by weight, preferably from 2 to 3% by weight, of DMAEE.
  • the DMAEE formed is removed by distillation from the main component, N,N-dimethylethanolamine, advantageously with a column operated continuously or batchwise within a temperature range (bottom) of from 40° C. to 150° C., preferably from 40° C. to 90° C., and at a pressure of from 5 to 1050 mbar, preferably from 5 to 300 mbar, more preferably from 10 to 150 mbar.
  • DMAEE is enriched in the bottom stream of this column.
  • the collected bottom stream is therefore fractionally distilled in a subsequent step.
  • Suitable column types for this distillation are all known column types, for example columns with random packing, tray columns, columns with structured packing and dividing wall columns. Preference is given to columns with structured packing and dividing wall columns.
  • DMAEE is distilled at relatively low pressures, for example in a thin-film evaporator, falling-film evaporator or short-path evaporator, or one of the latter apparatuses with attached column of any type, for example a column with structured packing.
  • the fractional distillation in a column is effected generally within a temperature range (bottom) of from 40 to 250° C., preferably from 135 to 235° C., in particular from 170 to 200° C.
  • the distillation is generally performed under reduced pressure, preferably within a range of from 1 to 1000 mbar, preferably from 100 to 500 mbar, more preferably 400 mbar.
  • the reflux ratio is generally from approx. 1.5:1 (reflux to withdrawal) to 5:1.
  • the distillation is effected at distillation temperatures of from 40 to 150° C., preferably from 40 to 100° C., and under a pressure of from 0.001 to 1 mbar, preferably from 0.01 to 0.1 mbar.
  • the DMAEE obtained in this step generally has a purity of ⁇ 98%, preferably ⁇ 99%, and a APHA color number of ⁇ 70, preferably ⁇ 20 APHA (see table 1).
  • the secondary components present are mainly small amounts of glycol, viny-loxyethanol and N,N-dimethylethanolamine, and slight discoloration, which is reestablished even after the distillation, is attributable essentially to traces of vinyloxyethanol.
  • vinyloxyethanol is therefore removed from DMAEE or destroyed by adding phosphorous acid, H 3 PO 3 .
  • either the DMAEE obtained in step c) can be subjected to a further distillation in which phosphorous acid is added, or the phosphorous acid is added actually in the course of the fractional distillation.
  • phosphorous acid in crystalline form or as a mixture of phosphorous acid and water. Both crystalline material and aqueous solutions are commercially available (for example from Supresta or Honeywell).
  • a mixture of phosphorous acid and water more preferably in a weight ratio of 1:10 to 10:1, in particular of 1:1.
  • from 0.01 to 10 parts by weight, preferably from 0.25 to 1 part by weight, of phosphorous acid per 25 parts by weight of the mixture to be distilled are used.
  • the distillation mixture is heat-treated with full reflux at a temperature of from 175 to 200° C., preferably from 180 to 190° C. and a pressure of from 400 to 600 mbar, preferably about 500 mbar, preferably for from 1 to 3 h, in particular about 2 h.
  • main secondary component glycol can be removed, for example, as a high-boiling acetal by adding a suitable higher aldehyde.
  • the resulting DMAEE is suitable, for example, as an intermediate for the synthesis of active pharmaceutical ingredients or a catalyst in polyurethane preparation.
  • the crude product of the industrial scale reaction of dimethylamine and ethylene oxide is subjected to a distillation to remove N,N-dimethylethanolamine.
  • the bottom residue of the column has the following composition in GC area %:
  • the dimethylaminoethoxyethanol obtained in fractions 6 to 8 corresponded to an isolated yield of about 72%.
  • the starting material was very dark in color. The distillation improved the color number significantly.
  • fractions 6 and 7 were combined and 250 g thereof were mixed with a mixture of 2.5 g of distilled water and 2.5 g of phosphorous acid H 3 PO 3 .
  • the homogeneous mixture was heat-treated at 185° C. for 2 hours and then distilled by means of a 20 cm column at 500 mbar and 182-184° C.
  • the 250 g of the crude material were mixed with a mixture of 10 g of distilled water and 10 g of phosphorous acid.
  • the bottom temperature in the column was adjusted to 145° C. with full reflux, and heating to reflux was continued for 2 h. After these 2 hours, a sample was taken from the column bottoms and the following composition was found:
  • fractional distillation was effected at column pressure 500 mbar, a ratio of reflux to efflux of approx. 5:1-2:1, bottom temperature 180° C. and distillation temperature 30-72° C., then 72-150° C.
  • Approx. 25% first runnings were removed, which consisted especially of methyldioxalane, N-methylmorpholine, N,N-dimethylethanolamine (DMEOA) and glycol.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)

Abstract

Processes comprising: (a) reacting dimethylamine and ethylene oxide to form a product mixture comprising N,N-dimethylethanolamine and N,N-dimethylaminoethoxyethanol; (b) distilling the product mixture to obtain a bottom fraction comprising N,N-dimethylaminoethoxyethanol; and (c) distilling the bottom fraction to separate at least a portion of the N,N-dimethylaminoethoxyethanol from the bottom fraction; and apparatus for carrying out said processes.

Description

  • The invention relates to a process for preparing N,N-dimethylaminoethoxyethanol, to an apparatus for performing it and to the use of by-products of the preparation of N,N-dimethylaminoethanol in such a process.
  • 2-[2-(dimethylamino)ethoxy]ethanol (N,N-dimethylaminoethoxyethanol, DMAEE) is a commercially available compound (BASF Corporation, USA), which finds use, for example, as an intermediate in the synthesis of active pharmaceutical ingredients or a catalyst in polyurethane preparation.
  • DMAEE is prepared firstly by reacting diethylene glycol with dimethylamine over a catalyst (see, for example, EP-A 0 303 323, JP-A 62/051646, JP-A 08/143,520 and JP-A 09/020,735), and secondly by reacting N,N-dimethylethanolamine with ethylene oxide (see, for example, J. G. Cannon et al., Journal of Pharmaceutical Sciences 62 (1973) 830 and U.S. Pat. No. 3,853,818).
  • Even though some of the processes mentioned are performed on the industrial scale, there is still a great deal of room for improvement, for example with regard to yields, selectivity, reaction times or simple workup.
  • It is an object of the invention to provide a process for preparing DMAEE which has advantages over the known processes at least in some aspects.
  • It has now been found that DMAEE forms in industrially utilizable amounts in the industrial preparation of N,N-dimethylethanolamine and can be removed in a simple manner in the purification of the N,N-dimethylethanolamine.
  • The invention therefore provides a process for preparing N,N-dimethylaminoethoxyethanol (DMAEE), wherein
    • a) dimethylamine and ethylene oxide are reacted,
    • b) the resulting product mixture of N,N-dimethylethanolamine and DMAEE is separated by distillation to obtain a DMAEE-containing fraction as the bottom stream, and
    • c) DMAEE from the fraction obtained in (b) is removed by distillation.
  • The invention further provides for the use of the bottom stream of a distillation of the reaction mixture of dimethylamine and ethylene oxide for obtaining DMAEE.
  • The invention likewise provides an apparatus for performing the above-described process, comprising (I) a reactor, preferably a tubular reactor, with inlets for dimethylamine and ethylene oxide and an outlet for the reaction product, (II) a distillation apparatus for enriching the DMAEE by distillatively removing N,N-dimethylethanolamine from the reaction mixture with an outlet for the DMAEE-containing bottom product at the bottom of the distillation apparatus and (III) an apparatus which is suitable for fractional distillation and has an inlet for the DMAEE-containing reaction mixture at the bottom or at the side and an outlet for the distilled DMAEE in the top region of the apparatus.
  • The process according to the invention can provide DMAEE in a simple manner and without complicated synthesis with catalysts and complex product mixtures. It is also advantageous that, to obtain a color-stable pure material, hydrogenation over a noble metal catalyst is not necessary.
  • The reaction of ethylene oxide and dimethylamine to give mainly N,N-dimethylethanolamine and its process parameters are known, and it is used on the industrial scale for the preparation of N,N-dimethylethanolamine. Details of this reaction step are described, for example, in DE-A 44 14 879.
  • The reaction mixture formed comprises generally from 1 to 6% by weight, preferably from 2 to 3% by weight, of DMAEE.
  • The DMAEE formed is removed by distillation from the main component, N,N-dimethylethanolamine, advantageously with a column operated continuously or batchwise within a temperature range (bottom) of from 40° C. to 150° C., preferably from 40° C. to 90° C., and at a pressure of from 5 to 1050 mbar, preferably from 5 to 300 mbar, more preferably from 10 to 150 mbar.
  • DMAEE is enriched in the bottom stream of this column.
  • To obtain pure DMAEE, the collected bottom stream is therefore fractionally distilled in a subsequent step.
  • Suitable column types for this distillation are all known column types, for example columns with random packing, tray columns, columns with structured packing and dividing wall columns. Preference is given to columns with structured packing and dividing wall columns. In a further preferred embodiment of the process, DMAEE is distilled at relatively low pressures, for example in a thin-film evaporator, falling-film evaporator or short-path evaporator, or one of the latter apparatuses with attached column of any type, for example a column with structured packing.
  • The fractional distillation in a column is effected generally within a temperature range (bottom) of from 40 to 250° C., preferably from 135 to 235° C., in particular from 170 to 200° C. The distillation is generally performed under reduced pressure, preferably within a range of from 1 to 1000 mbar, preferably from 100 to 500 mbar, more preferably 400 mbar. The reflux ratio is generally from approx. 1.5:1 (reflux to withdrawal) to 5:1.
  • In the further preferred embodiment of the process in a thin-film evaporator, falling-film evaporator or short-path evaporator, the distillation is effected at distillation temperatures of from 40 to 150° C., preferably from 40 to 100° C., and under a pressure of from 0.001 to 1 mbar, preferably from 0.01 to 0.1 mbar.
  • It is known to the person skilled in the art that relatively low distillation temperatures are possible with very good vacuum and the product can be distilled more gently as a result. In this distillation, it was found that, surprisingly, the DMAEE product remains stable even under relatively severe distillation conditions (see table 1) and could be isolated with very good yields and purities.
  • The DMAEE obtained in this step generally has a purity of ≧98%, preferably ≧99%, and a APHA color number of <70, preferably <20 APHA (see table 1). The secondary components present are mainly small amounts of glycol, viny-loxyethanol and N,N-dimethylethanolamine, and slight discoloration, which is reestablished even after the distillation, is attributable essentially to traces of vinyloxyethanol.
  • In a preferred embodiment of the invention, vinyloxyethanol is therefore removed from DMAEE or destroyed by adding phosphorous acid, H3PO3.
  • In this case, either the DMAEE obtained in step c) can be subjected to a further distillation in which phosphorous acid is added, or the phosphorous acid is added actually in the course of the fractional distillation.
  • It is possible to use the phosphorous acid in crystalline form or as a mixture of phosphorous acid and water. Both crystalline material and aqueous solutions are commercially available (for example from Supresta or Honeywell).
  • Preference is given to the addition of a mixture of phosphorous acid and water, more preferably in a weight ratio of 1:10 to 10:1, in particular of 1:1. In general, from 0.01 to 10 parts by weight, preferably from 0.25 to 1 part by weight, of phosphorous acid per 25 parts by weight of the mixture to be distilled are used.
  • The above-described advantage that DMAEE remains stable even at relatively high temperatures in the distillation is utilized especially in this preferred embodiment of the process because phosphorous acid H3PO3 is particularly active for the destruction of vinyloxyethanol (VOE) at elevated temperature. This reaction proceeds particularly advantageously at from 150° C. to 200° C. Especially at from 180° C. to 190° C., relatively small amounts of H3PO3 are required. For this reason, a distillation at from 400 to 600 mbar is particularly advantageous, because a bottom temperature of from 175 to 200° C., preferably from 180 to 190° C., is then established in the distillation.
  • In both variants, the distillation mixture is heat-treated with full reflux at a temperature of from 175 to 200° C., preferably from 180 to 190° C. and a pressure of from 400 to 600 mbar, preferably about 500 mbar, preferably for from 1 to 3 h, in particular about 2 h.
  • When the vinyloxyethanol is removed or destroyed in a separate distillation, this is preferably performed by means of a tray column, column with random packing, column with structured packing or dividing wall column, more preferably a column with structured packing or a dividing wall column under the pressure and temperature conditions specified above.
  • Further secondary components can be removed by known methods familiar to those skilled in the art; for example, the main secondary component glycol can be removed, for example, as a high-boiling acetal by adding a suitable higher aldehyde.
  • The resulting DMAEE is suitable, for example, as an intermediate for the synthesis of active pharmaceutical ingredients or a catalyst in polyurethane preparation.
  • The invention is illustrated in detail by the examples without thereby restricting it.
    • EXAMPLE 1 Distillation of the Bottom Stream of a Column for Removing N,N-Dimethylethanolamine
  • The crude product of the industrial scale reaction of dimethylamine and ethylene oxide is subjected to a distillation to remove N,N-dimethylethanolamine.
  • The bottom residue of the column has the following composition in GC area %:
  •
    Glycol:  6%
    Vinyloxyethanol:  4%
    N,N-dimethylethanolamine: 16%
    Dimethylaminoethoxyethanol: 74%
  • 918 g of this residue were subjected to a distillation by means of a 1 m column with random packing (diameter: 60 mm, random packings: 3×3 mm). The result is shown in table 1.
  • TABLE 1
    Distillation
    Fraction Fr. 1 Fr. 2 Fr. 3 Fr. 4 Fr. 5 Fr. 6 Fr. 7 Fr. 8
    Color number 11 APHA 7 APHA 26.5 APHA 25.5 APHA 7 APHA 5 APHA 13 APHA 68 APHA
    Weight in g 21 84 66 81 120 128 133 143
    Bottom T in ° C. 135-142 170-178 178-182 182 182-183 183 174-176 196-235
    Distillation T in ° C. 66-70  98-106 158-160 160 158-159 155-156 165-167 165-112
    Pressure in mbar 125-123 415-424 436-426 426-422 421 420-418 308-312 312-35 
    Reflux/efflux 05:02 05:02 10:01 10:02 10:02 10:02 04:02 03:02
    Composition
    GC area %
    Glycol 0.00 0.00 29.53 38.85 31.92 0.37 0.00 0.00
    Vinyloxyethanol 0.02 30.17 18.59 0.28 0.18 0.21 0.05 0.04
    Dimethylethanolamine 99.98 69.83 6.61 0.17 0.11 0.15 0.06 0.08
    DMAEE 0.00 0.00 45.27 60.7 67.79 99.27 99.89 99.88
    Total % 100.00 100.00 100.00 100.00 100.00 100.00 100.00 100.00
    Residue 94 g 29.26 49.13 81.07 124.99 131.87 141.70
  • The dimethylaminoethoxyethanol obtained in fractions 6 to 8 corresponded to an isolated yield of about 72%. The starting material was very dark in color. The distillation improved the color number significantly.
    • EXAMPLE 2 Distillation over H3PO3
  • From the distillation of example 1, fractions 6 and 7 were combined and 250 g thereof were mixed with a mixture of 2.5 g of distilled water and 2.5 g of phosphorous acid H3PO3. The homogeneous mixture was heat-treated at 185° C. for 2 hours and then distilled by means of a 20 cm column at 500 mbar and 182-184° C.
  • TABLE 2
    Distillation over H3PO3
    (Fr. 6 + Fr. 7) Distillate
    Color number (APHA) 19 0
    Composition GC area %
    Glycol 0.20 0.26
    Vinyloxyethanol 0.13 0.00
    Dimethylethanolamine 0.12 0.08
    DMAEE 99.55 99.66
    Total % 100.00 100.00
  • The treatment with phosphorous acid and subsequent distillation virtually quantitatively affords colorless N,N-dimethylaminoethoxyethanol (DMAEE) which, by GC, no longer comprises any vinyloxyethanol.
    • EXAMPLE 3
  • Combination of distillation and removal of vinyloxyethanol in a single step.
  • In a column with random packing (length: 1 m, diameter: 60 mm, 3×3 mm random packings, reflux divider, approx. 30 theoretical plates), 250 g of a crude material with the following composition were introduced into the still: 6.85% Glycol, 4.50% vinyloxyethanol, 15.20% dimethylethanolamine, 70.70% N,N-dimethylaminoethoxyethanol (DMAEE), 0.08% (dimethylaminoethyl) vinyl ether.
  • The 250 g of the crude material were mixed with a mixture of 10 g of distilled water and 10 g of phosphorous acid. The bottom temperature in the column was adjusted to 145° C. with full reflux, and heating to reflux was continued for 2 h. After these 2 hours, a sample was taken from the column bottoms and the following composition was found:
  • 0.01% vinyloxyethanol, 0.1% methanol, 1.69% methyldioxalane, 2.50% glycol, 6.44% N,N-dimethylethanolamine (DMEOA), 1.78% N-ethyl-N-methylethanolamine and 74.30% N,N-dimethylaminoethoxyethanol (DMAEE).
  • Subsequently, fractional distillation was effected at column pressure 500 mbar, a ratio of reflux to efflux of approx. 5:1-2:1, bottom temperature 180° C. and distillation temperature 30-72° C., then 72-150° C. Approx. 25% first runnings were removed, which consisted especially of methyldioxalane, N-methylmorpholine, N,N-dimethylethanolamine (DMEOA) and glycol.
  • Subsequently, the vacuum was lowered to 100 mbar, and distillation was continued at a bottom temperature of 138° C. rising up to 200-250° C., a constant distillation temperature of 130° C. and a ratio of reflux to efflux of 4:5. The pure product was obtained in a purity of 77-99%; the vinyloxyethanol (VOE) content in all pure fractions was significantly less than 0.1%. 145 g of the N,N-dimethylaminoethoxyethanol (DMAEE) product of value were obtained; this corresponds to approx. 82% yield based on the DMAEE present in the crude material (176 g) and 58% yield based on the total mass of the crude material used at the outset (250 g).

Claims (12)

1-10. (canceled)
11. A process comprising: (a) reacting dimethylamine and ethylene oxide to form a product mixture comprising N,N-dimethylethanolamine and N,N-dimethylaminoethoxyethanol; (b) distilling the product mixture to obtain a bottom fraction comprising N,N-dimethylaminoethoxyethanol; and (c) distilling the bottom fraction to separate at least a portion of the N,N-dimethylaminoethoxyethanol from the bottom fraction.
12. The process according to claim 11, wherein distilling the product mixture is carried out at a bottom temperature of 40 to 150° C. and at a pressure of 5 to 1050 bar.
13. The process according to claim 11, wherein distilling the bottom fraction comprises fractional distillation carried out in a column.
14. The process according to claim 13, wherein the fractional distillation is carried out at a bottom temperature of 40 to 280° C. and a pressure of 1 to 1000 mbar.
15. The process according to claim 1, wherein distilling the bottom fraction comprises fractional distillation carried out in one or more devices selected from the group consisting of a thin-film evaporator, a falling-film evaporator, and a short-path evaporator, optionally in conjunction with an attached column.
16. The process according to claim 15, wherein the distillation is carried out at a distillation temperature of 40 to 150° C. and at a pressure of 0.001 to 1 mbar.
17. The process according to claim 11, wherein phosphorous acid is added to the distillation of the bottom fraction.
18. The process according to claim 11, further comprising distilling the N,N-dimethylaminoethoxyethanol obtained from the bottom fraction over phosphorous acid.
19. An apparatus for carrying out the process according to claim 11, the apparatus comprising: (I) a tubular reactor an inlet for the dimethylamine, an inlet for the ethylene oxide, and an outlet for the product mixture; (II) a distillation apparatus for enriching the N,N-dimethylaminoethoxyethanol in the product mixture by distillatively removing N,N-dimethylethanolamine from the product mixture with an outlet for the bottom fraction at a bottom of the distillation apparatus; and (III) an apparatus which is suitable for fractional distillation and which has an inlet for the bottom fraction at a bottom or at a side of the apparatus, and an outlet at a top region of the apparatus for the distilled portion of N,N-dimethylethanolamine.
20. The apparatus according to claim 19, wherein the apparatus (III) suitable for fractional distillation comprises a column.
21. The apparatus according to claim 19, wherein the apparatus (III) suitable for fractional distillation comprises one or more devices selected from the group consisting of a thin-film evaporator, a falling-film evaporator, and a short-path evaporator, optionally in conjunction with an attached column.
US12/293,699 2006-03-20 2007-03-20 Process for preparing n,n-dimethylaminoethoxyethanol Abandoned US20090223805A1 (en)

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Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3131132A (en) * 1962-06-06 1964-04-28 Jefferson Chem Co Inc Purification of dimethylaminoethanol by acid treatment and distillation
US3853818A (en) * 1973-01-22 1974-12-10 Air Prod & Chem Aminoborate esters as polyurethane catalysts
US4049931A (en) * 1975-05-29 1977-09-20 Union Carbide Corporation Catalyst systems containing dimethylamino ether mono-ols for polyurethane foam formation
US4239855A (en) * 1978-07-21 1980-12-16 Texaco Development Corp. Polyurethane catalysts and method of use
US4847418A (en) * 1983-12-13 1989-07-11 Union Carbide Corporation Continuous process for preparing alkanolamines
US4922023A (en) * 1987-07-22 1990-05-01 Basf Aktiengesellschaft Preparation of aliphatic N,N-dialkyl-substituted amino alcohols
US5663444A (en) * 1994-04-28 1997-09-02 Basf Aktiengesellschaft Preparation of a pure dialkylaminoethanol stable against discoloration
US6521707B2 (en) * 2000-11-06 2003-02-18 Bayer Aktiengesellschaft Isocyanates containing amino groups

Family Cites Families (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3853A (en) 1844-12-12 Furnace of steam-boilers
US818A (en) 1838-06-30 Cheese-press
DE2810135A1 (en) 1978-03-09 1979-09-20 Basf Ag PROCESS FOR THE MANUFACTURING OF UNCOLORATED TECHNICAL AETHANOLAMINES
US4379024A (en) * 1981-07-23 1983-04-05 Pennwalt Corporation Process for the manufacture of alkylaminoalkanol
JPS6251646A (en) 1985-08-26 1987-03-06 ダブリユー・アール・グレイス・アンド・カンパニー−コネチカツト Alpha, omega-ditertiary amine
JPH08143520A (en) 1994-11-21 1996-06-04 Tosoh Corp How to aminate alcohol
JPH0920735A (en) 1995-07-11 1997-01-21 Tosoh Corp Amination method of alcohol

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3131132A (en) * 1962-06-06 1964-04-28 Jefferson Chem Co Inc Purification of dimethylaminoethanol by acid treatment and distillation
US3853818A (en) * 1973-01-22 1974-12-10 Air Prod & Chem Aminoborate esters as polyurethane catalysts
US4049931A (en) * 1975-05-29 1977-09-20 Union Carbide Corporation Catalyst systems containing dimethylamino ether mono-ols for polyurethane foam formation
US4239855A (en) * 1978-07-21 1980-12-16 Texaco Development Corp. Polyurethane catalysts and method of use
US4847418A (en) * 1983-12-13 1989-07-11 Union Carbide Corporation Continuous process for preparing alkanolamines
US4922023A (en) * 1987-07-22 1990-05-01 Basf Aktiengesellschaft Preparation of aliphatic N,N-dialkyl-substituted amino alcohols
US5663444A (en) * 1994-04-28 1997-09-02 Basf Aktiengesellschaft Preparation of a pure dialkylaminoethanol stable against discoloration
US6521707B2 (en) * 2000-11-06 2003-02-18 Bayer Aktiengesellschaft Isocyanates containing amino groups

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ATE537139T1 (en) 2011-12-15
US20120264979A1 (en) 2012-10-18
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EP1999102A1 (en) 2008-12-10

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