WO2020249428A1 - Produits obtenus par la conversion de dérivés du glycolaldéhyde et d'agents d'amination et leur conversion en éthylèneamines et éthanolamines - Google Patents

Produits obtenus par la conversion de dérivés du glycolaldéhyde et d'agents d'amination et leur conversion en éthylèneamines et éthanolamines Download PDF

Info

Publication number
WO2020249428A1
WO2020249428A1 PCT/EP2020/065201 EP2020065201W WO2020249428A1 WO 2020249428 A1 WO2020249428 A1 WO 2020249428A1 EP 2020065201 W EP2020065201 W EP 2020065201W WO 2020249428 A1 WO2020249428 A1 WO 2020249428A1
Authority
WO
WIPO (PCT)
Prior art keywords
glycolaldehyde
formula
hydrogen
derivative
alkyl
Prior art date
Application number
PCT/EP2020/065201
Other languages
English (en)
Inventor
Martin Ernst
Tatjana HUBER
Johann-Peter Melder
Stephanie JAEGLI
Thomas Krug
Original Assignee
Basf Se
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Basf Se filed Critical Basf Se
Priority to EP20730248.0A priority Critical patent/EP3983374B1/fr
Priority to US17/617,205 priority patent/US20220235015A1/en
Priority to BR112021022992A priority patent/BR112021022992A2/pt
Priority to CN202080044091.2A priority patent/CN114008016A/zh
Publication of WO2020249428A1 publication Critical patent/WO2020249428A1/fr

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C209/00—Preparation of compounds containing amino groups bound to a carbon skeleton
    • C07C209/24—Preparation of compounds containing amino groups bound to a carbon skeleton by reductive alkylation of ammonia, amines or compounds having groups reducible to amino groups, with carbonyl compounds
    • C07C209/26—Preparation of compounds containing amino groups bound to a carbon skeleton by reductive alkylation of ammonia, amines or compounds having groups reducible to amino groups, with carbonyl compounds by reduction with hydrogen
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C211/00—Compounds containing amino groups bound to a carbon skeleton
    • C07C211/01—Compounds containing amino groups bound to a carbon skeleton having amino groups bound to acyclic carbon atoms
    • C07C211/02—Compounds containing amino groups bound to a carbon skeleton having amino groups bound to acyclic carbon atoms of an acyclic saturated carbon skeleton
    • C07C211/03—Monoamines
    • C07C211/04—Mono-, di- or tri-methylamine
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C211/00—Compounds containing amino groups bound to a carbon skeleton
    • C07C211/01—Compounds containing amino groups bound to a carbon skeleton having amino groups bound to acyclic carbon atoms
    • C07C211/02—Compounds containing amino groups bound to a carbon skeleton having amino groups bound to acyclic carbon atoms of an acyclic saturated carbon skeleton
    • C07C211/03—Monoamines
    • C07C211/05—Mono-, di- or tri-ethylamine
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C211/00—Compounds containing amino groups bound to a carbon skeleton
    • C07C211/01—Compounds containing amino groups bound to a carbon skeleton having amino groups bound to acyclic carbon atoms
    • C07C211/02—Compounds containing amino groups bound to a carbon skeleton having amino groups bound to acyclic carbon atoms of an acyclic saturated carbon skeleton
    • C07C211/09—Diamines
    • C07C211/10—Diaminoethanes
    • 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
    • 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
    • C07C213/08—Preparation of compounds containing amino and hydroxy, amino and etherified hydroxy or amino and esterified hydroxy groups bound to the same carbon skeleton by reactions not involving the formation of amino groups, hydroxy groups or etherified or esterified hydroxy groups
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C215/00—Compounds containing amino and hydroxy groups bound to the same carbon skeleton
    • C07C215/02—Compounds containing amino and hydroxy groups bound to the same carbon skeleton having hydroxy groups and amino groups bound to acyclic carbon atoms of the same carbon skeleton
    • C07C215/04—Compounds containing amino and hydroxy groups bound to the same carbon skeleton having hydroxy groups and amino groups bound to acyclic carbon atoms of the same carbon skeleton the carbon skeleton being saturated
    • C07C215/06—Compounds containing amino and hydroxy groups bound to the same carbon skeleton having hydroxy groups and amino groups bound to acyclic carbon atoms of the same carbon skeleton the carbon skeleton being saturated and acyclic
    • C07C215/12—Compounds containing amino and hydroxy groups bound to the same carbon skeleton having hydroxy groups and amino groups bound to acyclic carbon atoms of the same carbon skeleton the carbon skeleton being saturated and acyclic the nitrogen atom of the amino group being further bound to hydrocarbon groups substituted by hydroxy groups
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07D—HETEROCYCLIC COMPOUNDS
    • C07D251/00—Heterocyclic compounds containing 1,3,5-triazine rings
    • C07D251/02—Heterocyclic compounds containing 1,3,5-triazine rings not condensed with other rings
    • C07D251/04—Heterocyclic compounds containing 1,3,5-triazine rings not condensed with other rings having no double bonds between ring members or between ring members and non-ring members
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07D—HETEROCYCLIC COMPOUNDS
    • C07D319/00—Heterocyclic compounds containing six-membered rings having two oxygen atoms as the only ring hetero atoms
    • C07D319/10—1,4-Dioxanes; Hydrogenated 1,4-dioxanes
    • C07D319/12—1,4-Dioxanes; Hydrogenated 1,4-dioxanes not condensed with other rings

Definitions

  • the present invention relates to processes for the manufacture of ethyleneamines and ethano lamines by hydrogenation of intermediates formed by the conversion of an aminating agent and a glycolaldehyde derivative.
  • the present invention further relates to a novel triazinane deriva tive, which is formed as an intermediate by the conversion of an aminating agent and a gly colaldehyde derivative.
  • Glycolaldehyde appears to be a useful raw material for the production of ethyleneamines and ethanolamines.
  • US 6,534,441 describes a process for reductive amination of lower aliphatic alkane derivatives using a nickel/rhenium catalyst.
  • a possible feedstock mentioned in the description is glycolalde hyde.
  • German patent application DE-A1 -4400591 describes a process for preparing amino alcohols by reacting hydroxy carbonyl compounds with hydrogen and an aminating agent at tempera tures of 0 to 300°C and pressures of 1 to 400 bar over a catalyst which comprises 50 to 100% by weight of ruthenium. Glycolaldehyde is disclosed as suitable hydroxy carbonyl compound which can be employed in the process.
  • CN 107011194 discloses a method for conversion of glycolaldehyde with different aminating agents, such as ammonia, methylamine, ethylamine and butylamine in the presence of hydro gen using noble metal catalysts which comprised rare earth metals.
  • aminating agents such as ammonia
  • WO2011/082994 discloses a method for conversion of glycolaldehyde with different aminating agents, such as ammonia, methylamine, ethylamine and butylamine in the presence of hydro gen using noble metal catalysts which comprised rare earth metals.
  • WO2011/082967 discloses the amination of glycolaldehyde with the aminating agents MEA and DEA in the presence of hydrogen and amination catalysts to yield alkanolamines.
  • the object of the present invention was to provide a process for the manufacture of eth- yleneamines and ethanolamines which give high yields based on the glycolaldehyde used in the reaction. It was a further object to obtain high degrees of conversion of glycolaldehyde and to obtain the desired ethyleneamines and ethanolamines with a high selectivity. It was a further object to provide a process for the conversion of glycolaldehyde which does not require the pre activation of catalysts as described in WO2011/082994.
  • the object of the present invention was achieved by a a process for the manufacture of ethyleneamines and ethanolamines, comprising the steps of
  • R 2 , R 3 are - the same or different -hydrogen, alkyl, such as Ci- 6 -alkyl, or cycloalkyl such as C 3-6 -cycloalkyl; and an aminating agent of formula (III); in which R 1 is hydrogen (H), alkyl, such as Ci- 6 -alkyl, or cycloalkyl such as C3-6- cycloalkyl, in the gas or liquid phase;
  • step (ii) feeding the reaction products obtained in step (i) into a hydrogenation reactor, where the reaction products are converted with hydrogen in the presence of a hydrogena tion catalyst.
  • glycolaldehyde derivative of formula (II) is converted with an aminating agent of formula (III).
  • alkyl such as Ci- 6 -alkyl, preferably Ci-4-alkyl, in particularly methyl, ethyl, n-propyl, iso-propyl, n- butyl, sec-butyl, tert-butyl and iso-butyl.
  • Cycloalkyl such as C3-6-cycloalkyl, preferably cyclopropyl, cyclobutyl, cyclopentyl and cyclohex yl ⁇
  • the glycolaldehyde derivative of formula (II) is glycolaldehyde, with R 2 and R 3 both being hydrogen residues (H).
  • Glycolaldehyde is commercially available and can be prepared, for example, by oxidizing eth ylene glycol (see, for example, JP 3246248 and JP 3279342).
  • Glycolaldehyde is preferably synthesized by reaction of formaldehyde with carbon monoxide and hydrogen, as described, for example, in US 2009012333, US 2008081931 ,
  • Glycolaldehyde can also be obtained from the cracking of biomass, such as sugars or wood, as disclosed in US 2004/0022912 or by D. Mohan et al. (“Pyrolysis of Wood/Biomass for Bio-Oil”, Energy Fuels 2006, 20, 3, 848-889) or by C. R. Vitasari (Extraction of bio-based glycolaldehyde from wood-derived pyrolysis oils Eindhoven: Technische Universiteit Eindhoven DOI:
  • the residue R 3 may be Hydrogen (H), alkyl, such as Ci- 6 -alkyl, preferably Ci-4-alkyl, in particularly methyl, ethyl, n-propyl, iso-propyl, n- butyl, sec-butyl, tert-butyl and iso-butyl.
  • alkyl such as Ci- 6 -alkyl, preferably Ci-4-alkyl, in particularly methyl, ethyl, n-propyl, iso-propyl, n- butyl, sec-butyl, tert-butyl and iso-butyl.
  • Cycloalkyl such as C3-6-cycloalkyl, preferably cyclopropyl, cyclobutyl, cyclopentyl and cyclohex yl ⁇
  • aminating agent of formula (III) is methylamine, ethylamine, n-propyl-amine, iso propyl amine, n-butylamine, sec-butylamine, tert-butylamine and iso-butylamine.
  • aminating agent of formula (III) is ammonia.
  • aminating agent and the glycolaldehyde derivative can be provided to step (i) in the gas or liquid form.
  • the glycolaldehyde is provided to step (i) in the liquid form.
  • glycolaldehyde derivatives of formula (II) are liquid at ambient temperatures.
  • Glycolaldehyde itself has a melting point of about 96-97°C and a boiling point of about 131 °C.
  • glycolaldehyde derivatives are provided to step (i) in the liquid form as a mixture in one or more solvents.
  • the solvent may be any solvent which is inert under the reaction conditions and has a sufficient solubility for the reactants.
  • the one or more solvents are selected from the group consisting of water, alcohols, non-cyclic or cyclic ethers, polyalkylethers and alkoxypolyalkylethers.
  • the one or more solvents are selected from the group consisting of water, methanol, ethanol, methyl tert-butyl ether, ethyl tert-butyl ether, dioxane, tetrahydrofuran, tetra- ethylene glycol dimethyl ether (tetraglyme), dipropylene glycol dimethyl ether (proglyme), bis(2- methoxyethyl) ether (diglyme) or other ethers of oligo- and polypropyleneoxides and oligo- and polyethyleneoxides or mixed oligo- or polyalkyleneoxides.
  • mixtures of water and tetrahydrofuran are used as solvents, wherein the molar ratio of water to THF is in the range of 1 :1 to 20:1 , more preferably 4:1 to 15:1 and most prefer ably 5:1 to 10:1.
  • mixtures of water and alkoxypolyalkylethers are used as solvents, where in the molar ratio of water to the alkoxypolyalkylethers are in the range of 200:1 to 100:10, more preferably 150:1 to 100:5 and most preferably 125:1 to 100:3.
  • the alkoxypoly alkylethers are selected from the group consisting of proglyme, diglyme and tetraglyme.
  • the concentration of the solutions of the glycolaldehyde derivatives of formula (II) are in the range of 1 to 95 preferably 10 to 85, more preferably 25 to 80 and most preferably 50 to 75 percent by weight, based on the weight of the glycolaldehyde derivative of formula (II) and the total weight of the one or more solvents in which the glycolaldehyde derivative of formula (II) is dissolved.
  • solutions of the glycolaldehyde derivative of formula (II) are obtained directly from a manufacturing process of the glycolaldehyde derivative of formula (II).
  • solutions may be obtained from the cracking of aqueous solutions of organic feedstocks at high temperatures and condensing the gaseous effluent obtained from such cracking reactions.
  • a glycolaldehyde solution is obtained by (i) the hydrous ther molysis of sugars, such as the process disclosed in US 2004/0022912, which is hereby incorpo rated by reference, and (ii) condensing the gaseous effluent from such a cracking process, or the processes described by D. Mohan et al. (“Pyrolysis of Wood/Biomass for Bio-Oil”, Energy Fuels 2006, 20, 3, 848-889) or by C. R. Vitasari (Extraction of bio-based glycolaldehyde from wood-derived pyrolysis oils Eindhoven: Technische Universiteit Eindhoven DOI:
  • the concentration of glycolaldehyde in such aqueous solutions is in the range of 5 to 80 percent by weight, most preferably 10 to 70 percent by weight and most preferably 25 to 60 percent by weight.
  • the aqueous solutions obtained by such processes may comprise other oxygenates, such as formaldehyde, hydroxyacetone (acetol), dihydroxyacetone, glyoxal, methylglyoxal (pyruvalde- hye), acetic acid, levulinic acid, propionic acid, acrylic acid, glycolic acid, methanol, acetone and formic acid.
  • oxygenates such as formaldehyde, hydroxyacetone (acetol), dihydroxyacetone, glyoxal, methylglyoxal (pyruvalde- hye), acetic acid, levulinic acid, propionic acid, acrylic acid, glycolic acid, methanol, acetone and formic acid.
  • One or more of the above listed solvents may be added to such aqueous glycolal dehyde solutions in amounts set out above before providing the aqueous solutions to step (i).
  • the glycolaldehyde derivative is provided to step (i) in the gas eous form.
  • the glycolaldehyde derivative is provided in the gaseous form by evapora tion of the liquid glycolaldehyde derivate in its pure form.
  • the glycolaldehyde derivative is provided in the gaseous form by evaporation of a solution of the glycolaldehyde derivative in one or more solvents. Evapora- tion from a solution is particularly preferred for those glycolaldehyde derivatives, which tend to form high boiling dimers, and which tend to oligomerize or polymerize upon heating.
  • Suitable solvents from which the glycolaldehyde derivative can be provided in the gaseous form are solvents which are inert under the reaction conditions and which have a sufficient solubility for the reactants.
  • the one or more solvents are selected from the group consisting of water, alcohols, non-cyclic or cyclic ethers, polyalkylethers and alkoxypolyalkylethers.
  • the one or more solvents are selected from the group consisting of water, methanol, ethanol, methyl tert-butyl ether, ethyl tert-butyl ether, dioxane, tetrahydrofuran, tetra- ethylene glycol dimethyl ether (tetraglyme), dipropylene glycol dimethyl ether (proglyme) or bis(2-methoxyethyl) ether (diglyme).
  • mixtures of water and tetrahydrofuran are used as solvents, wherein the molar ratio of water to THF is in the range of 1 :1 to 20:1 , more preferably 4:1 to 15:1 and most prefer ably 5:1 to 10:1.
  • even more preferably mixtures of water, THF and alkoxypolyalkylethers are used as solvents, wherein the molar ratio of water to the alkoxypolyalkylethers are in the range of 200:1 to 100:10, more preferably 150:1 to 100:5 and most preferably 125:1 to 100:3 and the ratio of water to THF is in the range described above.
  • the alkoxypolyalkylethers are selected from the group consisting of proglyme, diglyme and tetraglyme.
  • the concentration of the solutions of the glycolaldehyde derivatives of formula (II) from which the glycolaldehyde derivative is evaporated from are in the range of 1 to 80 prefera bly 2.5 to 50, more preferably 5 to 30 and most preferably 5 to 20 percent by weight, based on the weight of the glycolaldehyde derivative of formula (II) and the total weight of the one or more solvents in which the glycolaldehyde derivative of formula (II) is dissolved.
  • the concentration of the solutions from which the glycolaldehyde derivative is evaporated from are usually lower than the concentration of the solutions used for the liquid phase reaction, because glycolaldehyde has a tendency to oligomerize and polymerize during the evaporation process.
  • Evaporation of the glycolaldehyde derivate of formula (II) or their respective solutions may be performed by operations well-known in the arts, e.g. by heating the liquids to temperatures above the boiling point of the glycolaldehyde derivative of formula (II) and/or by reducing the pressure and or by passing a stream of gas over the liquid glycolaldehyde derivative of formula (I I).
  • the glycolaldehyde derivative of formula (II) transferred into the gas phase by evapo ration by heating in a stream of gas.
  • the gas is preferably hydrogen or an inert gas, such as nitrogen or a noble gas, such as He, Ne Ar, Kr or Xe.
  • the gas is hydrogen, nitrogen or a mixture thereof.
  • Evaporators which can be used for the evaporation of the glycolaldehyde derivative and their respective solutions are natural or forced circulation evaporators, falling film evaporators, rising film (or long tube vertical) evaporators, climbing and falling-film plate evaporators, multi-effect evaporators, and agitated thin film evaporators.
  • the evaporation can also be performed by a flash evaporation.
  • the glycolaldehyde derivative of formula (II) in the gaseous form is directly provided by a manufacturing process in which the glycolaldehyde derivative of formula (II) is produced.
  • Such gaseous streams may be obtained from the cracking of aqueous solutions of organic feedstocks at high temperatures.
  • a glycolaldehyde solution is obtained by the hydrous thermol ysis of sugars, such as the process disclosed in US 2004/0022912, which is hereby incorpo rated by reference.
  • the concentration of glycolaldehyde in such gaseous streams in this preferred em bodiment is preferably in the range of 5 to 80 percent by weight, most preferably 10 to 70 per cent by weight and most preferably 25 to 60 percent by weight.
  • the gaseous streams obtained by such processes may comprise other oxygenates, such as formaldehyde, hydroxyacetone (acetol), dihydroxyacetone, glyoxal, methylglyoxal (pyruvalde- hyde), acetic acid, levulinic acid, propionic acid, acrylic acid, glycolic acid, methanol, acetone and formic acid.
  • oxygenates such as formaldehyde, hydroxyacetone (acetol), dihydroxyacetone, glyoxal, methylglyoxal (pyruvalde- hyde), acetic acid, levulinic acid, propionic acid, acrylic acid, glycolic acid, methanol, acetone and formic acid.
  • aminating agent of formula (III) may also be provided to step (i) in the gas or liquid form.
  • aminating agent is used in its liquid form, it is preferably used in its pure form.
  • the aminating agent may also be provided in form of its solution in one or more solvents.
  • the one or more solvents are the same as the solvents used for the preparation of the solutions of the glycolaldehyde derivative. More preferably, aqueous solutions of the aminating agent are being provided to step (i).
  • the concentration of the aminating agent in the solutions is preferably in the range of 5 to 75 percent by weight, more preferably 10 to 60 percent by weight and more preferably 15 to 35 percent by weight, based on the total weight of aminating agents and the sum of all solvents used for the solutions.
  • the aminating agent may also be provided in the gaseous form.
  • aminating agents such as ammonia, methylamine and ethylamine exist in a gaseous form under ambient conditions.
  • aminating agents may be transferred to the gas phase by evaporation of the aminating agents in their pure form or by evaporation of the aforementioned solutions of the aminating agents.
  • the molar ratio of the glycolaldehyde derivative of formula (II) and the aminating agent is pref erably in the range of 1 :1 to 100:1 , more preferably in the range of 1 :1 to 25:1 and most prefer ably in the range of 1 : 1 to 15: 1.
  • the conversion of the glycolaldehyde derivative and the aminating agent are preferably carried out under conditions in which hydrogenation or reductive amination of the glycolaldehyde deriv ative of formula (II), the aminating agent of formula (III) and any reaction products of the aminat ing agent and glycolaldehyde derivative, in particular any triazinane derivative of formula (I) and any diamino dioxane derivative of formula (IV), is substantially impeded or suppressed.
  • such conditions comprise the absence of a hydrogenation catalyst and/or hydrogen in step (i). If hydrogen is present in step (i), step (i) is preferably conducted in the absence of a hydrogenation catalyst.
  • step (i) is preferably conducted in the absence of hydrogen. If both hydrogen and a hydrogenation catalyst are pre sent during step (i), the reaction condition described below - especially the temperature - is selected to be in a range in which hydrogenation is effectively suppressed, e.g. ambient tem peratures. Hydrogenation and reductive amination are substantially impeded, if only minor amounts of ethyleneamines, such as ethylenediamine, and alkanolamines, such monoethano- lamine and diethanolamine, are formed during step (i).
  • ethyleneamines such as ethylenediamine
  • alkanolamines such monoethano- lamine and diethanolamine
  • the conversion is preferably carried out under conditions as to substantially prevent the gly- colaldehyde derivative from oxidation. It is thus preferred to that the reaction is carried out under inert conditions, preferably in a sealed system or more preferably under a stream of an inert gas, such as hydrogen, nitrogen or a noble gas, such as He, Ne Ar, Kr or Xe or mixtures there of.
  • an inert gas such as hydrogen, nitrogen or a noble gas, such as He, Ne Ar, Kr or Xe or mixtures there of.
  • the conversion of the glycolaldehyde derivative and the aminating agent may be performed in the liquid phase.
  • the conversion of the glycolaldehyde derivative and the aminating agent may be performed continuously, batch-wise or semi-continuously.
  • the conversion may be carried out in one or a series of reactors suitable for liquid phase reac tions.
  • tubular reactors Preference is given to tubular reactors, reactors with external or internal recirculation, plug flow reactors, spray reactors, reaction columns, and stirred tank reactors.
  • the conversion is carried out in a tubular reactor.
  • the conversion is carried out in a stirred tank re actor
  • the reactants may be mixed before entering the reactor (pre-mixing) or they may be mixed in side the reactor.
  • Mixing may occur by feeding the feed streams into a suitable reactor or a common pipe leading to a suitable reactor. Mixing may be facilitated by using conventional equipment, such as pipes, nozzles, valves, stat ic mixers, agitators, stirrers, flow-meters, pumps, carrier-gases and the like.
  • the conversion of the glycolaldehyde derivative and the aminating agent in the liquid phase is preferably carried out in the range -25 to 150°C, more preferably -10 to 100°C and most prefer ably 0 to 75°C.
  • Conversion in the liquid phase is preferably performed under a pressure in the range of 0.5 to 100 bar, more preferably 0.8 to 50 and most preferably 1 to 20 bar.
  • the conversion in the liquid phase is conducted at a pressure of about 1 bar and at ambient temperatures, such as temperatures in the range of 0 to 30°C.
  • the conversion of the glycolaldehyde derivative and the aminating agent is carried out in the gas phase.
  • the conversion of the glycolaldehyde derivative and the aminating agent may be performed continuously, batchwise or semi-continuously.
  • the conversion may be carried out in one or a series of reactors suitable for gas phase reac tions.
  • tubular reactors Preference is given to tubular reactors, reactor chambers, or reactors with external or internal recirculation.
  • the conversion is carried out in a tubular reactor or a reaction chamber.
  • the gaseous reactants may be mixed before entering the reactor (pre-mixing) or they may be mixed inside the reactor.
  • Mixing may occur by feeding the gaseous feed streams into a suitable reactor or a common pipe leading to a suitable reactor.
  • Mixing in the gas-phase may be facilitated by using conventional equipment, such as pipes, nozzles, valves, static mixers, flow-meters, pumps, carrier-gases and the like.
  • the conversion in the gas phase is preferably carried out in the range 50 to 300°C, more pref erably 60 to 250°C and most preferably 80 to 200°C. Conversion in the gas phase is preferably performed under a pressure in the range of 0.1 to 200 bar, more preferably 0.5 to 100 bar, more preferably 1 to 30 bar and most preferably 1 to 20 bar.
  • glycolaldehyde derivatives of formula (II) and aminating agents of formula (III) may lead to at least two different types of reaction products.
  • each R 1 , each R 2 and each R 3 residue may be different. This may be the case if a mixture of different glycolaldehyde derivatives of formula (II) and a mixture of different ami nating agents of formula (III) are used as starting materials.
  • each R 1 , each R 2 and each R 3 are the same
  • each R 1 , each R 2 and each R 3 is hydrogen
  • the present invention is also directed to a triazinane derivative of formula (I).
  • each R 1 , each R 2 and each R 3 residue may be different. This may be the case if a mixture of different glycolaldehyde derivatives of formula (II) and a mixture of different ami- nating agents of formula (III) are used as starting materials.
  • each R 1 , each R 2 and each R 3 are the same
  • each R 1 , each R 2 and each R 3 is hydrogen.
  • Figures 1 and 2 show the nuclear magnetic resonance spectrum ( 1 H-NMR and 13 C-NMR) of the compound of formula (V)
  • reaction products of step (i) should not be limited to the specific structures disclosed above.
  • reaction products obtained in a gas phase reaction by the conversion of the glycolaldehyde derivative of formula (II) and the aminating agent of formula (III) are usually high boiling prod ucts which tend to desublimate or condensate from the gas phase in solid or liquid form.
  • Separation of a solid or liquid from the gas phase can be carried out using conventional means, such as inertial separators (cyclone, settling chamber, vortex chamber) or wet separators (ven turi scrubbers, jet scrubbers, scrubbing columns) using a scrubbing liquid.
  • useful scrubbing liquid are liquids, in which the reaction product of the glycolaldehyde derivative and the aminating agent have a sufficient solubility.
  • the scrubbing liquids are selected from the group consisting of water, alcohols, non- cyclic or cyclic ethers, polyalkylethers and alkoxypolyalkylethers.
  • the one or more scrubbing liquids is selected from the group consisting of wa ter, methanol, ethanol, methyl tert-butyl ether, ethyl tert-butyl ether, dioxane, tetrahydrofuran, tetraethylene glycol dimethyl ether (tetraglyme), dipropylene glycol dimethyl ether (proglyme) or bis(2-methoxyethyl) ether (diglyme).
  • separation of the reaction products from the gas phase is carried out by condensa tion or desublimation of the reaction product.
  • Condensation or desublimation is preferably car ried out by feeding the gas stream to a heat exchanger.
  • Heat exchangers can be shell and tube heat exchangers or plate heat exchangers, preferably heat exchangers.
  • the heat exchangers used for the condensation or desublimation are preferably incorporated as a by-pass into the process and can thus be easily disconnected, cleaned and incorporated again, while the process is running.
  • the cleaning of the heat exchangers on the side facing the process stream is usually conducted with a scrubbing liquid which detaches the adhering by-products to achieve a cleaning effect.
  • the by-products are preferably completely or partly dissolved and removed as solution or slurry from the heat exchanger.
  • the speed of the cleaning by dissolution and discharge of the prod ucts is promoted by increasing the flow rate of the scrubbing liquid during the cleaning process or by scrubbing with a heated scrubbing liquid, to increase the solubility of the reaction products in the scrubbing liquid.
  • the conversion of the glycolaldehyde derivative and the aminating agent in step (i) is carried out in the presence of one or more scrubbing liquids.
  • the scrubbing liquid is usually evaporated together with the aminating agent or the glycolaldehyde derivative and provided to step (i) in gaseous form.
  • the scrubbing liquids are also condensed at the heat exchang ers. The condensation of the scrubbing liquid on the heat exchangers has the effect that any desublimated or condensed reaction products are intrinsically washed off from the heat ex changers.
  • reaction products obtained in a liquid phase reaction may be obtained as solutions in the one or more solvents present during step (i), or the reaction products obtained in a liquid phase reac tion may at least partially precipitate from the liquid phase.
  • Separation of a solid from the liquid phase can be carried out using conventional means such as filtration, in particular cross-flow filtration, sedimentation or centrifugation.
  • the solutions Prior to liquid-solid separation, the solutions may be concentrated by evaporating at least a part of the one or more solvents present during the reaction mixture or by cooling the solutions.
  • solvent which is a precipitating agent for the reaction products may be added to facilitated liquid-solid separation.
  • precipitating agents are nonpolar solvents, such as aliphatic hydrocar bons or aromatic hydrocarbons such as hexane, heptane, octane, cyclohexane, toluene or xy lene.
  • reaction products from the conversion of the glycolaldehyde derivative and the aminating agent in the gas or liquid phase may be obtained in a solid form or as dispersions or solutions in the one or more solvent present during the conversion and/or the scrubbing liquid used during work-up.
  • reaction products are obtained in step (i) as solutions or as dispersions of the reaction products in one or more solvent, the dispersions or the solutions may be directly fed into the hydrogenation step (ii).
  • the solutions or dispersions obtained from step (i) may be concen trated by evaporating at least part of the solvent comprised in such solutions to obtain a concen trated solution, a slurry or even a resinous solid.
  • This embodiment has the advantage that sol vents which have a lower hydrogen solubility can be at least partially removed and replaced against solvents having a higher hydrogen solubility.
  • reaction products are obtained in the solid form, it is preferred to dissolve the reaction products in one more solvent before feeding the reaction products into step (ii).
  • the concentrated solutions, slurry or resinous solids of the reaction products obtained after the concentration step can be compounded with one or more solvents.
  • the one or more solvents are selected from the group consisting of water, alcohols, non-cyclic or cyclic ethers, polyalkylethers and alkoxypolyalkylethers.
  • the one or more solvents are selected from the group consisting of water, methanol, ethanol, methyl tert-butyl ether, ethyl tert-butyl ether, dioxane, tetrahydrofuran, tetra- ethylene glycol dimethyl ether (tetraglyme), dipropylene glycol dimethyl ether (proglyme) or bis(2-methoxyethyl) ether (diglyme).
  • the one or more solvent which is added has a higher hydrogen solubility than the solvent removed in the concentration step previously described.
  • water can be partially removed and replaced by methanol to yield mixtures of the reaction products in water and methanol.
  • reaction products formed during step (i), especially the triazinane deriva tive of formula (I) and/or the diamino dioxane derivative of formula (iv) are useful as intermedi ates for the preparation of ethyleneamines and ethanolamines.
  • reaction products of the aminating agent and the glycolaldehyde derivate obtained in step (i) are fed into a hydrogenation reactor, where the reaction products from step (i) are converted with hydrogen in the presence of a hydrogenation catalyst.
  • reaction products obtained from step (i) comprise diamino dioxane derivatives of formula (IV) and triazinane derivatives of formula (I).
  • the reaction products obtained in step (i) may also comprise other adducts of the aminating agent and the glycolaldehyde derivative having a dif ferent structure than the triazinane or the diamino dioxane derivates.
  • reaction products obtained in step (i) comprise 75 to 100 per cent by weight, more preferably 80 to 100 percent by weight and most preferably 90 to 100 per cent by weight of triazinane derivatives of formula (I). In a further preferred embodiment, the reaction products obtained in step (i) comprise 75 to 100 percent by weight, more preferably 80 to 100 percent by weight and most preferably 90 to 100 percent by weight of diamino dioxane derivatives of formula (IV).
  • reaction products obtained in step (i) comprise
  • the present invention is also directed to a process for the manufacture of eth- yleneamines and ethanolamines by converting a triazinane derivative of formula (I) and/or a diamino dioxane derivative of formula (IV) with hydrogen in a hydrogenation reactor in the pres ence of a hydrogenation catalyst.
  • reaction products obtained in step (i) are fed to the step (ii) in form of their solu tions in one or more solvents.
  • the one or more solvents are water,
  • ethers preferably methyl tert-butyl ether, ethyl tert-butyl ether, dioxane or tetrahydrofuran (THF), and
  • alcohols preferably methanol, ethanol and iso-propanol.
  • Useful solvents also include suitable mixtures of the solvents listed above.
  • Particularly preferred solvents are methanol, THF, dioxane, glymes and water.
  • Particularly preferred solvents also include the reaction products of step (ii), such monethano- lamine (MEOA), diethanolamine (DEOA), triethanolamine (TEOA) and ethylenediamine (EDA).
  • MEOA monethano- lamine
  • DEOA diethanolamine
  • TEOA triethanolamine
  • EDA ethylenediamine
  • the concentration of the reaction products, which are fed to step (ii) in the one or more solvents is preferably in the range of 1 to 100 g reaction products per 100 g of solvents, more preferably 5 to 75 g reaction products per 100 g of solvents and most preferably 10 to 50 g reaction prod ucts per 100 g of solvents
  • the hydrogenation step (ii) is carried out in the presence of hydrogen.
  • the hydrogen is generally used in technical grade purity.
  • the hydrogen can also be used in the form of a hydrogen-comprising gas, i.e. with additions of other inert gases, such as nitrogen, helium, neon, argon or carbon dioxide.
  • hydrogen having a content of more than 99% by weight of hydrogen, preferably more than 99.9% by weight of hydrogen, more prefera- bly more than 99.99% by weight of hydrogen, especially more than 99.999% by weight of hy drogen may be used in step (ii).
  • the partial pressure of hydrogen in step (ii) is preferably in the range of 2.5 to 200 bar, more preferably 5 to 150 bar and even more preferably 10 to 100 bar and most preferably 20 to 50 bar.
  • the hydrogenation step (ii) is conducted in the presence of an acid.
  • the presence of acids increases the yields of desired products, such as eth- yleneamines and alkanolamines.
  • the acid can be any organic or inorganic acid.
  • Non-limiting examples of such organic carboxylic acids are: saturated aliphatic monocarboxylic acids,
  • hydroxy carboxylic acids such as hydroxy acetic acid, hydroxy propionic acid, ethylidene lactic acid, hydroxy butyric acid, a-hydroxy isobutryric acid, hydroxy caproic acid, hydroxy stearic acid, tartronic acid, tartaric acid, malic acid, hydroxy benzoic acid and the like.
  • acids of the aforementioned groups comprise the monocarboxylic acids containing from 1 to 8 carbon atoms, in particular formic acid, acetic acid, propionic acid, butyric acid, valeric acid, caproic acid, enanthic acid, caprylic acid, pelargonic acid, capric acid dicarboxylic acids containing from 2 to 8 carbon atoms, in particular oxalic acid, maleic acid, succinic acid, glutaric acid, adipic acid, pimelic acid, suberic acid, azelaic acid, sebacic acid, hydroxy-carboxylic acids from 2 to 8 carbon atoms, in particular glycolic acid, lactic acid, citric acid and mandelic acid
  • the one or more organic carboxylic acids are selected from the group consist ing of formic acid, acetic acid, lactic acid, glycolic acid, levulinic acid, acrylic acid and pyruvic acid.
  • the concentration of acids present during the hydrogenation step (ii) is preferably in the range of 0.1 to 25 percent by weight, more preferably 0.5 to 20 percent by weight and most preferably 1 to 10 percent by weight, based on the total weight of the feed stream fed into the hydrogena tion step (ii).
  • the hydrogenation step (ii) is conducted in the presence of ammonia.
  • Ammonia may already be present in the effluent stream coming from step (i).
  • step (ii) additional ammonia may be added to step (ii).
  • the amount of ammonia present during the hydrogenation step (ii) is in the range of 1 to 50 percent by weight, preferably 5 to 40 percent by weight and more preferably 10 to 30 per cent by weight, based on the total weight of the feed stream fed into the hydrogenations step.
  • the hydrogenation step (ii) is conducted in the presence of a hydrogenation catalyst.
  • the hydrogenation catalysts may in principle comprise nickel, cobalt, iron, copper, chromium, manganese, copper, molybdenum, tungsten and/or other metals of groups 8 and/or 9 and/or 10 and/or 11 of the periodic table of the elements
  • hydrogenation catalysts which comprise at least one metal selected from the group consisting of Cu, Co, Ni, Pd, Pt, Ru, Rh, Ag, Au, Re and Ir.
  • hydrogenation catalysts which comprise at least one metal selected from the group consisting of Cu, Co, Ni, Pd, Pt and Ru.
  • the abovementioned catalysts can be doped in a customary manner with promoters, for exam ple with chromium, iron, cobalt, manganese, molybdenum, titanium, tin, metals of the alkali metal group, metals of the alkaline earth metal group and/or phosphorus.
  • the hydrogenation catalyst can be a supported or unsupported catalyst.
  • Suitable support materials are carbon compounds such as graphite, carbon black and/or acti vated carbon, aluminum oxide (gamma, delta, theta, alpha, kappa, chi or mixtures thereof), sili con dioxide, zirconium dioxide, zeolites, aluminosilicates or mixtures thereof.
  • Raney catalysts As Raney catalysts, Raney cobalt catalysts, Raney nickel catalysts and / or Raney copper cata lysts are preferably used. Raney cobalt catalysts are particularly preferred.
  • the hydrogenation catalysts are prepared by reduction of a catalyst precursor, in which the aforementioned metals are present in the form of oxygen comprising compounds, such as their oxides, carbonates or hydrogencarbonates.
  • the catalyst precursors can be prepared by known processes, for example by precipitation, precipitative application or impregnation.
  • catalyst precursors which are prepared by impregnating support materials are used in the process according to the invention (impregnated catalyst precursors).
  • the support materials used in the impregnation can, for example, be used in the form of pow ders or shaped bodies, such as extrudates, tablets, spheres or rings.
  • Support material suitable for fluidized bed reactors is preferably obtained by spray drying.
  • Useful support materials include, for example, carbon such as graphite, carbon black and/or activated carbon, aluminum oxide (gamma, delta, theta, alpha, kappa, chi or mixtures thereof), silicon dioxide, zirconium dioxide, zeolites, aluminosilicates or mixtures thereof.
  • support materials can be impregnated by the customary methods (A. B. Stiles, Catalyst Manufacture - Laboratory and Commercial Preparations, Marcel Dekker, New York, 1983), for example by applying a metal salt solution in one or more impregnation stages.
  • Useful metal salts generally include water-soluble metal salts, such as the nitrates, acetates or chlorides of the corresponding catalytically active components or the doping elements, such as cobalt nitrate or cobalt chloride. Thereafter, the impregnated support material is generally dried and optionally calcined.
  • the impregnation can also be performed by the so-called "incipient wetness method", in which the support material is moistened with the impregnating solution up to a maximum of saturation according to its water absorption capacity.
  • the impregnation can also be performed in supernatant solution.
  • Multistage impregnation can be employed ad vantageously when the support material is to be contacted with metal salts in a relatively large amount.
  • the impregnation can be per formed simultaneously with all metal salts or in any desired sequence of the individual metal salts.
  • catalyst precursors are prepared by means of a coprecipita tion of all of their components.
  • a soluble compound of the corresponding active component and of the doping elements, and optionally a soluble compound of a support material is admixed with a precipitant in a liquid while heating and while stirring until the precipi tation is complete.
  • the liquid used is generally water.
  • Useful soluble compounds of the active components typically include the corresponding metal salts, such as the nitrates, sulfates, acetates or chlorides of the aforementioned metals.
  • the soluble compounds of a support material used are generally water-soluble compounds of Ti, Al, Zr, Si etc., for example the water-soluble nitrates, sulfates, acetates or chlorides of these elements.
  • the soluble compounds of the doping elements used are generally water-soluble compounds of the doping elements, for example the water-soluble nitrates, sulfates, acetates or chlorides of these elements.
  • Catalyst precursors can also be prepared by precipitative application.
  • Precipitative application is understood to mean a preparation method in which a sparingly solu ble or insoluble support material is suspended in a liquid and then soluble compounds, such as soluble metal salts, of the appropriate metal oxides, are added, which are then precipitated onto the suspended support by adding a precipitant (for example, described in EP-A2-1 106 600, page 4, and A. B. Stiles, Catalyst Manufacture, Marcel Dekker, Inc., 1983, page 15).
  • a precipitant for example, described in EP-A2-1 106 600, page 4, and A. B. Stiles, Catalyst Manufacture, Marcel Dekker, Inc., 1983, page 15).
  • Useful sparingly soluble or insoluble support materials include, for example, carbon compounds such as graphite, carbon black and/or activated carbon, aluminum oxide (gamma, delta, theta, alpha, kappa, chi or mixtures thereof), silicon dioxide, zirconium dioxide, zeolites, aluminosili cates or mixtures thereof.
  • the support material is generally present in the form of powder or spall.
  • the liquid used, in which the support material is suspended is typically water.
  • Useful soluble compounds include the aforementioned soluble compounds of the active compo nents or of the doping elements. Typically, in the precipitation reactions, the soluble compounds are precipitated as sparingly soluble or insoluble basic salts by adding a precipitant.
  • the precipitants used are preferably alkalis, especially mineral bases, such as alkali metal ba ses.
  • examples of precipitants are sodium carbonate, sodium hydroxide, potassium carbonate or potassium hydroxide.
  • the precipitants used may also be ammonium salts, for example ammonium halides, ammoni um carbonate, ammonium hydroxide or ammonium carboxylates.
  • the precipitation reactions can be performed, for example, at temperatures of 20 to 100°C, preferably 30 to 90°C, especially at 50 to 70°C.
  • the precipitates formed in the precipitation reactions are generally chemically inhomogeneous and generally comprise mixtures of the oxides, oxide hydrates, hydroxides, carbonates and/or hydrogencarbonates of the metals used. It may be found to be favorable for the filterability of the precipitates when they are aged, i.e. when they are left alone for a certain time after the precipitation, if appropriate under hot conditions or while passing air through.
  • the precipitates obtained by these precipitation processes are typically processed by washing, drying, calcining and conditioning them.
  • the precipitates are generally dried at 80 to 200°C, preferably 100 to 150°C, and then calcined.
  • the calcination is performed generally at temperatures between 300 and 800°C, preferably 350 to 600°C, especially at 450 to 550°C.
  • the pulverulent catalyst precursors obtained by precipitation reactions are typically conditioned.
  • the conditioning can be affected, for example, by adjusting the precipitation catalyst to a partic ular particle size by grinding.
  • the catalyst precursor obtained by precipitation reactions can be mixed with shaping assistants such as graphite or stearic acid and processed further to shaped bodies.
  • shaping assistants such as graphite or stearic acid
  • Common processes for shaping are described, for example, in Ullmann [Ullmann’s Encyclopae dia Electronic Release 2000, chapter: “Catalysis and Catalysts", pages 28-32] and by Ertl et al. [Ertl, Knozinger, Weitkamp, Handbook of Heterogeneous Catalysis, VCH Weinheim, 1997, pag es 98 ff].
  • the process for shaping can provide shaped bodies in any three-dimensional shape, for example round, angular, elongated or the like, for example in the form of extrudates, tablets, granules, spheres, cylinders or grains.
  • Common processes for shap ing are, for example, extrusion, tableting, i.e. mechanical pressing, or pelletizing, i.e. compact ing by circular and/or rotating motions.
  • the conditioning or shaping is generally followed by a heat treatment.
  • the temperatures in the heat treatment typically correspond to the temperatures in the calcination.
  • the catalyst precursors obtained by precipitation reactions comprise the catalytically active components in the form of a mixture of oxygen compounds thereof, i.e. especially as the oxides, mixed oxides and/or hydroxides.
  • the catalyst precursors thus prepared can be stored as such.
  • the hydrogenation catalyst which is used in the process according to the invention is obtained by reducing catalyst precursors which have been prepared by impregnation or precipitation as described above after the calcination or conditioning.
  • the reduction of the dry, generally pulverulent catalyst precursor can be performed at elevated temperature in a moving or stationary reduction oven.
  • the reducing agent used is typically hydrogen or a hydrogen-comprising gas.
  • the hydrogen is generally used in technical grade purity.
  • the hydrogen can also be used in the form of a hydrogen-comprising gas, i.e. in admixtures with other inert gases, such as nitrogen, helium, neon, argon or carbon dioxide.
  • the hydrogen stream can also be recycled into the re duction as cycle gas, optionally mixed with fresh hydrogen and optionally after removing water by condensation.
  • the catalyst precursor is preferably reduced in a reactor in which the shaped catalyst bodies are arranged as a fixed bed.
  • the catalyst precursor is more preferably reduced in the same re actor in which step (ii) is carried out.
  • the catalyst precursor can be reduced in a fluidized bed reactor in the fluidized bed.
  • the catalyst precursor is generally reduced at reduction temperatures of 50 to 600°C, especially of 100 to 500°C, more preferably of 150 to 450°C.
  • the partial hydrogen pressure is generally from 1 to 300 bar, especially from 1 to 200 bar, more preferably from 1 to 100 bar, where the pressure figures here and hereinafter are based on the absolute measured pressure.
  • the duration of the reduction is preferably 1 to 20 hours and more preferably 5 to 15 hours.
  • a solvent can be supplied in order to remove water of reaction which forms and/or in order, for example, to be able to heat the reactor more rapidly and/or to be able to better remove the heat during the reduction.
  • the solvent can also be supplied in supercritical form.
  • Suitable solvents used may be the above-described solvents.
  • Preferred solvents are water; ethers such as methyl tert-butyl ether, ethyl tert-butyl ether, dioxane or tetrahydrofuran. Particu lar preference is given to water or tetrahydrofuran.
  • Suitable solvents likewise include suitable mixtures.
  • the catalyst precursor can also be reduced in suspension, for example in a stirred autoclave.
  • the temperatures are generally within a range from 50 to 300°C, especially from 100 to 250°C, more preferably from 120 to 200°C.
  • the reduction in suspension is generally performed at a partial hydrogen pressure of 1 to 300 bar, preferably from 10 to 250 bar, more preferably from 30 to 200 bar.
  • the duration of the reduction in suspension is preferably 5 to 20 hours, more preferably 8 to 15 hours.
  • the catalyst can be handled under inert conditions after the reduction.
  • the catalyst can prefer ably be handled and stored under an inert gas such as nitrogen, or under an inert liquid, for ex ample an alcohol, water or the product of the particular reaction for which the catalyst is used. If appropriate, the catalyst must then be freed of the inert liquid before commencement of the ac tual reaction.
  • the storage of the catalyst under inert substances enables uncomplicated and safe handling and storage of the catalyst.
  • the catalyst can also be contacted with an oxygen-comprising gas stream such as air or a mixture of air with nitrogen.
  • an oxygen-comprising gas stream such as air or a mixture of air with nitrogen.
  • the passivated catalyst generally has a protective oxide layer. This protective oxide layer simplifies the handling and storage of the catalyst, such that, for example, the installation of the passivated catalyst into the reactor is simplified.
  • the catalyst is usually activated.
  • a catalyst can be activated by reducing a passivated catalyst.
  • a passivated catalyst can be reduced as described above by treating the passivated catalyst with hydrogen or a hydrogen-comprising gas.
  • the reduction conditions cor respond generally to the reduction conditions employed in the reduction of the catalyst precur sors.
  • the activation generally eliminates the protective passivation layer.
  • An activated catalyst has to be handled under inert conditions during and after the activating reduction thereof.
  • the activated catalyst is preferably handled and stored under an inert gas, such as nitrogen, or under an inert liquid, for example an alcohol, water or the product of the particular reaction for which the catalyst is used. If appropriate, the activated catalyst then has to be freed of the inert liquid before commencement of the actual reaction.
  • an inert gas such as nitrogen
  • an inert liquid for example an alcohol, water or the product of the particular reaction for which the catalyst is used. If appropriate, the activated catalyst then has to be freed of the inert liquid before commencement of the actual reaction.
  • Activation of the catalyst can also occur in situ during the hydrogenation step (ii).
  • reaction products of step (i) are contacted with a reduced or activated hydrogenation catalyst.
  • Step (ii) is performed in a hydrogenation reactor.
  • the process according to the invention can be performed continuously, batchwise or semicon- tinuously.
  • Typical reactors are, for example, high-pressure stirred tank reactors, autoclaves, fixed bed re actors, fluidized bed reactors, moving beds, circulating fluidized beds, salt bath reactors, plate heat exchangers as reactors, staged reactors with a plurality of stages with or without heat ex change and removal/supply of substreams between the trays, in possible embodiments as radi- al flow or axial flow reactors, continuous stirred tanks, bubble reactors, etc., the reactor used in each case being that suitable for the desired reaction conditions (such as temperature, pressure and residence time).
  • the process according to the invention is preferably performed in a high-pressure stirred tank reactor, fixed bed reactor or fluidized bed reactor.
  • the process according to the invention is performed in one or more fixed bed reactors.
  • reaction products from step (i) are hydrogen ated in a high-pressure stirred tank reactor.
  • the hydrogenation is typically performed at a pressure of 1 to 500 bar, preferably 10 to 350 bar, more preferably at a pressure of 50 to 300 bar and most preferably 80 to 220 bar.
  • the pressure is maintained or controlled generally via the metered addition of the hydrogen.
  • the hydrogenation generally proceeds at temperatures of 15 to 350°C, preferably 50 to 250°C, more preferably 80 to 220°C.
  • the residence time in the hydrogenation step in the case of performance in a batchwise pro cess, is generally 15 minutes to 72 hours, preferably 60 minutes to 24 hours, more preferably 2 hours to 10 hours.
  • the catalyst hourly space velocity is generally in the range from 0.01 kg of reaction products obtained in step (i)/kg of catalyst/h to 3.0 kg of reaction products obtained in step (i)/kg of catalyst/h, preferably 0.05 kg of reaction products obtained in step (i)/kg of catalyst/h to 2.0 kg of reaction products obtained in step (i)/kg of catalyst/h and more preferably 0.1 kg of reaction products obtained in step (i)/kg of catalyst/h - 1.5 kg of reaction products obtained in step (i)/kg of catalyst/h.
  • the effluent of the hydrogenation step comprises unreacted products, hydrogen, solvent, eth- yleneamines and ethanolamines.
  • the effluent may optionally also comprise acids and/or ammonia.
  • ethyleneamines produced in the hydrogenation step (ii) are ethylenediamine (EDA), monoethanolamine (MEOA), diethanolamine (DEOA).
  • ethyleneamines such as diethylentriamine (DETA), triethylenetetramine (TETA), pipera zine (PIP) and aminoethylethanolamine (AEEA) may also be formed in smaller quantities.
  • DETA diethylentriamine
  • TETA triethylenetetramine
  • PIP pipera zine
  • AEEA aminoethylethanolamine
  • the effluent of the hydrogenation step may be subjected to one or more work -up steps, such as hydrogen removal, ammonia removal solvent removal and distillation to obtain the respective ethyleneamines and ethanolamines in purified form.
  • the distillation may be conducted as a se quence of distillation steps using conventional distillation columns or divided wall columns.
  • the destillative work-up of ethyleneamines is well-established in the state of the art and can be found in further detail in the Process Economic Program Report No. 138“Alkyl Amines” pub lished by SRI International, Menlo Park, California, March 1981.
  • a basic substance may be added to the effluent prior to distillation in an amount sufficient to convert the acids into a high boiling salt.
  • the advantages of the present invention are that it has been possible to develop a process for converting glycolaldehyde which enables a high conversion of glycolaldehyde and the formation of products, especially of MEOA, DEOA and/or EDA, in high yield and selectivity.
  • the formation of the undesired piperazine by-product is reduced.
  • the conversion products are obtained in a high purity.
  • these in termediates constitute a stabilized form of glycolaldehyde and show a reduced tendency to par ticipate in undesired side reactions, such as oligomerization or polymerization.
  • the intermedi ates can be hydrogenated in a second step in the presence of hydrogen and a hydrogenation catalyst to provide the desired ethyleneamines and ethanolamines in high yields.
  • Example 1 Conversion of glycolaldehyde and ammonia in the gas phase (Step (i)): Gaseous glycolaldehyde was provided by evaporation of an aqueous solution of the glycolalde hyde dimer in THF (7.5 wt.-% glycolaldehyde dimer, 11.5 wt.-% THF, 80 wt.-% water and 1 wt- % tetraglyme) by heating the solution to 160°C in a tube evaporator comprising Raschig-rings. The gaseous feed was fed into an unheated reaction chamber operated at ambient pressure.
  • THF 7.5 wt.-% glycolaldehyde dimer, 11.5 wt.-% THF, 80 wt.-% water and 1 wt- % tetraglyme
  • Gaseous ammonia at room temperature was also fed to the reaction chamber through a sepa rate inlet.
  • the product solution was analyzed with GC and yielded a distinct product peak, which was identical to the peak obtained by performing a GC on the crystals.
  • the other substances in the product solutions were identified to be the solvents (THF, water, tetraglyme) from which the gly- colaldehyde was evaporated from and excess ammonia.
  • Example 2 Hydrogenation of the reaction products obtained from Example 1 (Step (ii)): 35 g of the product solution obtained from Example 1 were transferred to an autoclave.
  • the autoclave was pressurized to 20 bar and was heated to 80°C.
  • the autoclave was pressurized with hydrogen to a pressure of 100 bar.
  • composition of the product solution was analyzed by gas chromatography.
  • Example 3 Hydrogenation of the reaction products obtained from Example 1 (Step (ii)):
  • Example 3 was identical to Example 2, with the exception that an additional 10 g of ammonia was added to the autoclave at 20 °C and the solution was stirred for 1 h at 80 °C before the autoclave was pressurized to 100 bar with hydrogen gas
  • composition of the product solution was analyzed by gas chromatography.
  • MEG monoethylene glycol
  • Example 5 Hydrogenation of the reaction products obtained from Example 4 (Step (ii)):
  • Example 4 The solid residue obtained in Example 4 was dissolved in 50 ml of methanol.
  • the autoclave was pressurized to 20 bar and was heated to 80°C.
  • the autoclave was pressurized with hydrogen to a pressure of 100 bar.
  • composition of the product solution was analyzed by gas chromatography.
  • Example 6 Hydrogenation of the reaction products obtained from Example 4 (Step (ii)):
  • Example 6 was identical to Example 5, with the exception that an additional 15 g of ammonia were added to the autoclave at 20 °C and the solution was stirred for 1 h at 80 °C before the autoclave was pressurized to 100 bar with hydrogen gas.
  • composition of the product solution was analyzed by gas chromatography.
  • MEG monoethylene glycol
  • Glycolaldehyde was converted with aqueous ammonia as described in Example 1 of US 4,667,213.
  • Example 8 Hydrogenation of the reaction products obtained from Example 7 (Step (ii)):
  • the solution was then transferred to an autoclave and was pressurized with hydrogen to a pressure of 20 bar at 20 °C..
  • the autoclave was heated to 100°C.
  • the autoclave was pressurized with hydrogen to a pressure of 100 bar.
  • composition of the product solution was analyzed by gas chromatography.
  • Example 9 Hydrogenation of the reaction products obtained from Example 7 (Step (ii)):
  • Example 9 was identical to Example 8, with the exception that an additional 14 g of ammonia were added to the autoclave.
  • composition of the product solution was analyzed by gas chromatography.
  • MEG monoethylene glycol
  • Example 10 Hydrogenation of the reaction products obtained from Example 7 (Step (ii)):
  • Example 10 was identical to Example 9, with the exception that only 2.7 g of the precipitate from Example 7 were dissolved in 60 ml of methanol and 7.6 g of ammonia were charged to the au- toclave.
  • the hydrogenation catalyst was a mixture of 0.5 g of a Raney cobalt catalyst and 1 g of a catalyst consisting of PO2..
  • composition of the product solution was analyzed by gas chromatography.
  • MEG monoethylene glycol
  • Example 11 Hydrogenation of the reaction products obtained from Example 7 (Step (ii)) in the presence of an acid:
  • Example 11 was identical with example 9, with the exception that 0.34 g acetic acid were addi tionally added to the autoclave.
  • composition of the product solution was analyzed by gas chromatography.
  • MEG monoethylene glycol

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

L'invention concerne un procédé de fabrication d'éthylèneamines et d'éthanolamines, comprenant les étapes consistant à (i) convertir un dérivé du glycolaldéhyde de formule (II), dans laquelle R2, R3 sont identiques ou différents et représentent l'hydrogène, un alkyle, tel qu'un alkyle en C1-6, ou un cycloalkyle, tel qu'un Cs-e-cycloalkyle ; et un agent d'animation de formule (III), dans laquelle R1 représente l'hydrogène (H), un alkyle, tel qu'un alkyle en C1-6, ou un cycloalkyle, tel qu'un cycloalkyle en C3-6, dans la phase gazeuse ou liquide ; (ii) introduire les produits de réaction obtenus à l'étape (i) dans un réacteur d'hydrogénation, les produits de réaction étant convertis en hydrogène en présence d'un catalyseur d'hydrogénation.
PCT/EP2020/065201 2019-06-11 2020-06-02 Produits obtenus par la conversion de dérivés du glycolaldéhyde et d'agents d'amination et leur conversion en éthylèneamines et éthanolamines WO2020249428A1 (fr)

Priority Applications (4)

Application Number Priority Date Filing Date Title
EP20730248.0A EP3983374B1 (fr) 2019-06-11 2020-06-02 Produits obtenus par la conversion de dérivés de glycolaldéhyde et d'agents d'amination et leur conversion en éthylèneamines et éthanolamines
US17/617,205 US20220235015A1 (en) 2019-06-11 2020-06-02 Products obtained by the conversion of glycolaldehyde derivatives and aminating agents and their conversion to ethyleneamines and ethanolamines
BR112021022992A BR112021022992A2 (pt) 2019-06-11 2020-06-02 Processos para a fabricação de etilenoaminas e etanolaminas e derivado de triazinano
CN202080044091.2A CN114008016A (zh) 2019-06-11 2020-06-02 通过乙醇醛衍生物和胺化剂的转化以及它们向亚乙基胺类和乙醇胺类的转化获得的产物

Applications Claiming Priority (6)

Application Number Priority Date Filing Date Title
EP19179444 2019-06-11
EP19179444.5 2019-06-11
EP19179445 2019-06-11
EP19179449 2019-06-11
EP19179449.4 2019-06-11
EP19179445.2 2019-06-11

Publications (1)

Publication Number Publication Date
WO2020249428A1 true WO2020249428A1 (fr) 2020-12-17

Family

ID=66821096

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP2020/065201 WO2020249428A1 (fr) 2019-06-11 2020-06-02 Produits obtenus par la conversion de dérivés du glycolaldéhyde et d'agents d'amination et leur conversion en éthylèneamines et éthanolamines

Country Status (1)

Country Link
WO (1) WO2020249428A1 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2023135035A1 (fr) 2022-01-14 2023-07-20 Basf Se Procédé de fabrication ou de conversion d'alcanolamines

Citations (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4322568A (en) 1979-05-14 1982-03-30 Weiss Alvin H Glycolaldehyde or ethylene glycol from formaldehyde
US4503260A (en) 1983-06-13 1985-03-05 Monsanto Company Glycolaldehyde process
US4667213A (en) 1984-09-24 1987-05-19 Rca Corporation Charge-coupled device channel structure
US4677213A (en) 1983-11-22 1987-06-30 Research Association For Utilization Of Light Oil 2,5-diamino-1,4-dioxane derivatives and process for production thereof
DE4400591A1 (de) 1994-01-12 1995-07-13 Basf Ag Verfahren zur Herstellung von Aminoalkoholen
US6147261A (en) 1998-11-23 2000-11-14 Shell Oil Corporation Diaminoalkane syntheses via selective amination of hydroxyaldehydes
EP1106600A2 (fr) 1999-12-06 2001-06-13 Basf Aktiengesellschaft Procédé pour la préparation d'amines
JP3246248B2 (ja) 1995-01-25 2002-01-15 株式会社イトーキクレビオ パネルの遮音構造
JP3279342B2 (ja) 1992-04-17 2002-04-30 ソニー株式会社 ビデオカメラにおける手振れ補正装置
US6534441B1 (en) 1999-03-06 2003-03-18 Union Carbide Chemicals & Plastics Technology Corporation Nickel-rhenium catalyst for use in reductive amination processes
US20040022912A1 (en) 2000-11-20 2004-02-05 Majerski Piotr A Production of glycolaldehyde by hydrous thermolysis of sugars
EP1697291A1 (fr) 2003-12-16 2006-09-06 Shell Internationale Researchmaatschappij B.V. Procede pour la preparation de glycolaldehyde
US20080081931A1 (en) 2006-09-29 2008-04-03 Eastman Chemical Company Process for the preparation of glycolaldehyde
WO2011082994A1 (fr) 2009-12-17 2011-07-14 Basf Se Conversion de glycolaldéhyde avec un agent d'amination
WO2011082967A1 (fr) 2009-12-17 2011-07-14 Basf Se Procédé de préparation d'éthanolamines supérieures
CN107011194A (zh) 2016-01-27 2017-08-04 中国科学院大连化学物理研究所 一种由乙醇醛还原胺化制备醇胺及二胺的方法

Patent Citations (18)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4322568A (en) 1979-05-14 1982-03-30 Weiss Alvin H Glycolaldehyde or ethylene glycol from formaldehyde
US4503260A (en) 1983-06-13 1985-03-05 Monsanto Company Glycolaldehyde process
US4677213A (en) 1983-11-22 1987-06-30 Research Association For Utilization Of Light Oil 2,5-diamino-1,4-dioxane derivatives and process for production thereof
US4667213A (en) 1984-09-24 1987-05-19 Rca Corporation Charge-coupled device channel structure
JP3279342B2 (ja) 1992-04-17 2002-04-30 ソニー株式会社 ビデオカメラにおける手振れ補正装置
DE4400591A1 (de) 1994-01-12 1995-07-13 Basf Ag Verfahren zur Herstellung von Aminoalkoholen
JP3246248B2 (ja) 1995-01-25 2002-01-15 株式会社イトーキクレビオ パネルの遮音構造
US6147261A (en) 1998-11-23 2000-11-14 Shell Oil Corporation Diaminoalkane syntheses via selective amination of hydroxyaldehydes
US6534441B1 (en) 1999-03-06 2003-03-18 Union Carbide Chemicals & Plastics Technology Corporation Nickel-rhenium catalyst for use in reductive amination processes
EP1106600A2 (fr) 1999-12-06 2001-06-13 Basf Aktiengesellschaft Procédé pour la préparation d'amines
US20040022912A1 (en) 2000-11-20 2004-02-05 Majerski Piotr A Production of glycolaldehyde by hydrous thermolysis of sugars
EP1697291A1 (fr) 2003-12-16 2006-09-06 Shell Internationale Researchmaatschappij B.V. Procede pour la preparation de glycolaldehyde
US20070249871A1 (en) 2003-12-16 2007-10-25 Shell Oil Company Process of Preparing Glycolaldehyde
US20090012333A1 (en) 2003-12-16 2009-01-08 Almeida Lenero Karina Quetzaly Process of Preparing Glycolaldehyde
US20080081931A1 (en) 2006-09-29 2008-04-03 Eastman Chemical Company Process for the preparation of glycolaldehyde
WO2011082994A1 (fr) 2009-12-17 2011-07-14 Basf Se Conversion de glycolaldéhyde avec un agent d'amination
WO2011082967A1 (fr) 2009-12-17 2011-07-14 Basf Se Procédé de préparation d'éthanolamines supérieures
CN107011194A (zh) 2016-01-27 2017-08-04 中国科学院大连化学物理研究所 一种由乙醇醛还原胺化制备醇胺及二胺的方法

Non-Patent Citations (7)

* Cited by examiner, † Cited by third party
Title
"Catalysis and Catalysts", ULLMANN'S ENCYCLOPAEDIA ELECTRONIC RELEASE, 2000, pages 28 - 32
"Process Economic Program Report No. 138", March 1981, SRI INTERNATIONAL, article "Alkyl Amines"
C. R. VITASARI, EXTRACTION OF BIO-BASED GLYCOLALDEHYDE FROM WOOD-DERIVED PYROLYSIS OILS EINDHOVEN: TECHNISCHE UNIVERSITEIT EINDHOVEN
D. MOHAN ET AL.: "Pyrolysis of Wood/Biomass for Bio-Oil", ENERGY FUELS, vol. 20, no. 3, 2006, pages 848 - 889
ERTLKNOZINGERWEITKAMP: "Handbook of Heterogeneous Catalysis", 1997, VCH, pages: 98
LIANG ET AL., ANGEW. CHEM., vol. 129, 2017, pages 3096 - 3100
PELCKMANS, ACS CATAL., vol. 8, 2018, pages 4201 - 4212

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2023135035A1 (fr) 2022-01-14 2023-07-20 Basf Se Procédé de fabrication ou de conversion d'alcanolamines

Similar Documents

Publication Publication Date Title
RU2480449C2 (ru) Способ получения аминов из глицерина
US8742174B2 (en) Method for preparing higher ethanolamines
US9353032B2 (en) Method for the production of neopentyl glycol
US20090030237A1 (en) Method for producing ethylene amines and ethanol amines by the hydrogenating amination of monoethylene glycol and ammonia in the presence of a catalyst
EP3983374B1 (fr) Produits obtenus par la conversion de dérivés de glycolaldéhyde et d'agents d'amination et leur conversion en éthylèneamines et éthanolamines
JP6049757B2 (ja) 液相中での第二級アミンの製造法
TWI468377B (zh) 製造新戊二醇之連續方法
JPH01299239A (ja) ネオペンチルグリコールの製造方法
CN111971269B (zh) 乙醇醛的反应
SG190750A1 (en) Method for producing and purifying 3-aminopropanol
CN107986974A (zh) 一种制备环己烷二甲胺的方法
CN111871459B (zh) 一种改性催化剂及其制备方法、制备n,n-二甲基-1，3-丙二胺的方法
CN113024351A (zh) 一种异丙醇的生产方法
US4248799A (en) Hydrogenation of nitriles in ammonia and water
WO2020249428A1 (fr) Produits obtenus par la conversion de dérivés du glycolaldéhyde et d'agents d'amination et leur conversion en éthylèneamines et éthanolamines
WO2020249426A1 (fr) Conversion de glycolaldéhyde avec un agent d'amination
CN114014768A (zh) 一种无钡盐杂质的氨甲环酸及其制备方法和制剂组合物
US9695121B2 (en) 2,6-bis-(aminomethyl)piperidine derivatives
CN114471572A (zh) 一种用于二元腈加氢制二元胺的催化剂、其制备方法和应用
CN116003775B (zh) 三胺基聚醚化合物及其制备方法和应用
CN108290826B (zh) 基于聚合物质量的氨基酸或酯的组合物和获得其的方法
JPH03193738A (ja) ネオペンチルグリコールの製造方法

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 20730248

Country of ref document: EP

Kind code of ref document: A1

REG Reference to national code

Ref country code: BR

Ref legal event code: B01A

Ref document number: 112021022992

Country of ref document: BR

NENP Non-entry into the national phase

Ref country code: DE

ENP Entry into the national phase

Ref document number: 112021022992

Country of ref document: BR

Kind code of ref document: A2

Effective date: 20211116

ENP Entry into the national phase

Ref document number: 2020730248

Country of ref document: EP

Effective date: 20220111