EP2185499A1 - Procédé pour produire des amines à partir de glycérine - Google Patents

Procédé pour produire des amines à partir de glycérine

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Publication number
EP2185499A1
EP2185499A1 EP08787269A EP08787269A EP2185499A1 EP 2185499 A1 EP2185499 A1 EP 2185499A1 EP 08787269 A EP08787269 A EP 08787269A EP 08787269 A EP08787269 A EP 08787269A EP 2185499 A1 EP2185499 A1 EP 2185499A1
Authority
EP
European Patent Office
Prior art keywords
piperazine
glycerol
catalyst
aminomethyl
group
Prior art date
Legal status (The legal status 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 status listed.)
Withdrawn
Application number
EP08787269A
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German (de)
English (en)
Inventor
Martin Ernst
Bram Willem Hoffer
Johann-Peter Melder
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
BASF SE
Original Assignee
BASF SE
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Filing date
Publication date
Application filed by BASF SE filed Critical BASF SE
Priority to EP08787269A priority Critical patent/EP2185499A1/fr
Publication of EP2185499A1 publication Critical patent/EP2185499A1/fr
Withdrawn legal-status Critical Current

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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
    • C07C209/04—Preparation of compounds containing amino groups bound to a carbon skeleton by substitution of functional groups by amino groups
    • C07C209/14—Preparation of compounds containing amino groups bound to a carbon skeleton by substitution of functional groups by amino groups by substitution of hydroxy groups or of etherified or esterified hydroxy groups
    • C07C209/16—Preparation of compounds containing amino groups bound to a carbon skeleton by substitution of functional groups by amino groups by substitution of hydroxy groups or of etherified or esterified hydroxy groups with formation of amino groups bound to acyclic carbon atoms or to carbon atoms of rings other than six-membered aromatic rings
    • 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
    • C07C213/02—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 involving the formation of amino groups from compounds containing hydroxy groups or etherified or esterified hydroxy groups
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07D—HETEROCYCLIC COMPOUNDS
    • C07D295/00—Heterocyclic compounds containing polymethylene-imine rings with at least five ring members, 3-azabicyclo [3.2.2] nonane, piperazine, morpholine or thiomorpholine rings, having only hydrogen atoms directly attached to the ring carbon atoms
    • C07D295/02—Heterocyclic compounds containing polymethylene-imine rings with at least five ring members, 3-azabicyclo [3.2.2] nonane, piperazine, morpholine or thiomorpholine rings, having only hydrogen atoms directly attached to the ring carbon atoms containing only hydrogen and carbon atoms in addition to the ring hetero elements
    • C07D295/023—Preparation; Separation; Stabilisation; Use of additives

Definitions

  • the present invention relates to a process for the preparation of amines from glycerol and their use. Furthermore, the present invention relates to 1,2,3-triamino propane, 2-aminomethyl-6-methylpiperazine, 2,5-bis (aminomethyl) piperazine and 2,6-bis (aminomethyl) piperazine and their preparation by hydrogenating amination of glycerin.
  • the large-scale production of technically important aminoalkanols such as ethanolamine and isopropanolamine, and their secondary products, such as ethylenediamine, 1,2-propylenediamine and piperazine, are generally based on ethylene oxide or propylene oxide as the C2 or C3 synthetic building block.
  • the monoalkanolamines thus obtained can be further reacted by reaction of hydrogen and ammonia to ethylenediamine or 1,2-propylenediamine.
  • 1, 3-diaminopropane is industrially available by reacting ammonia with acrylonitrile and subsequent hydrogenation, acrylonitrile is usually produced industrially by ammoxidation of the C3 block propene.
  • raw materials based on renewable raw materials could become more important.
  • glycerin which is a by-product of fat saponification and of biodiesel production, could become increasingly important.
  • polyether amines already commercially available amines based on glycerol are the so-called polyether amines.
  • the synthesis of polyetheramines by amination of polyalkylenediols or triols is described, for example, in the review article by Fischer et al. (Fischer, T. Mallat, A. Baiker, Catalysis Today, 37 (1997), 167-189).
  • poly- For example, alkylene triols can be obtained by reaction of ethylene oxide or propylene oxide with glycerine.
  • glycerol is first oxidized to 2,3-dihydroxypropionic acid (glyceric acid) and subsequently in the presence of hydrogen and ammonia over a catalyst system consisting of a mixture of carbon-supported palladium and ruthenium, reductively aminated to DL-serine.
  • glycerol is oxidized only to the dihydroxyacetone and then, as described above, reacted in a reductive amination reaction to serinol (2-amino-1, 3-propanediol), which is then further oxidized to serine.
  • serinol (2-amino-1, 3-propanediol)
  • serine 2,3-amino-1, 3-propanediol
  • the decomposition products glycine or monoethanolamine can be formed by dehydrogenation and decarbonylation reactions.
  • the present invention was based on the object to use glycerol as a source for the production of amines.
  • a process should be provided that allows both technical amines and special glycerol-based amines and piperazine derivatives to be obtained in order to optimally utilize the raw material glycerine.
  • Technical amines are those amines which are usually obtained on the basis of petrochemical raw materials, for example monoamines, such as methylamine, ethylamine, i-propylamine or n-propylamine,
  • Diamines such as ethylenediamine, 1, 2-propanediamine or 1, 3-propanediamine, alkanolamines, such as monoethanolamine, 2-aminopropan-1-ol or 1-aminopropan-2-ol, or piperazine.
  • Glycerol-based special amines are amines which are characterized in that at least one OH group of the glycerol is substituted by a primary amino group, a secondary amino group or a tertiary amino group, for example 1, 2,3-triaminopropane, 1, 3-diaminopropane-2 -ol, 1, 2-diaminopropan-3-ol, 1-aminopropanediol or 2-aminopropanediol.
  • These compounds have a high number of functionalities and can therefore represent important intermediates in the synthesis of organic compounds such as crop protection agents, pharmaceuticals, stabilizers, etc.
  • Piperazine derivatives such as 2-methylpiperazine, 2,6-dimethylpiperazine, 2,5-dimethylpiperazine, 2,5-bis (aminomethyl) piperazine, 2,6-bis (amino methyl) - piperazine, 2-aminomethyl-5-methylpiperazine and 2-aminomethyl-6-methylpiperazine can also be important building blocks of the synthesis.
  • the conversion of glycerol to said compounds should involve only a few reaction steps in order to keep the investment costs as low as possible.
  • adjustments to the process conditions such as pressure and temperature, reaction time, catalyst loading, variation of the molar amination to glycerol ratio, as well as by the selection of the catalyst used, it should also be possible within certain limits the composition of the reaction In order to respond better to demand and sales fluctuations in relation to technical amines, special glycerol-based or piperazine derivatives.
  • a process for the preparation of amines by reacting glycerol with hydrogen and an aminating agent selected from the group of ammonia, primary and secondary amines, in the presence of a catalyst at a temperature of 100 0 C to 400 0 C and a pressure of 0, 01 to 40 MPa (0.1 to 400 bar) found.
  • the educts used in the reaction are glycerol, hydrogen and an aminating agent selected from the group consisting of ammonia, primary and secondary amines.
  • Glycerol is usually a by-product in the conversion of fats and oils to fatty acids (fat saponification) or fatty acid methyl esters (biodiesel).
  • fat saponification fatty acids
  • biodiesel fatty acid methyl esters
  • the production of glycerol from fats and oils is described, for example, in Ullmann (Ullmann's Encyclopedia of Industrial Chemistry, Glycerol, Chapter 4.1 "Glycerol from Fat and Oils", Wiley-VCH Verlag, Electronic Edition, 2007).
  • Glycerine can also be prepared starting from the petrochemical starting product propene.
  • An overview of the synthesis of glycerol from propene is also given in Ullmann (Ullmann's Encyclopedia of Industrial Chemistry, "Glycerol”, Chapter 4.1 "Synthesis from Propene", Wiley-VCH-Verlag, Electronic Edition, 2007).
  • Ullmann Ullmann's Encyclopedia of Industrial Chemistry, "Glycerol”, Chapter 4.1 "Synthesis from Propene”, Wiley-VCH-Verlag, Electronic Edition, 2007.
  • Both glycerol on a vegetable, animal or petrochemical basis is suitable as a starting material for the process according to the invention.
  • glycerol based on renewable raw materials for example glycerol, which is obtained as a by-product from fat saponification or biodiesel production.
  • Glycerol is available in various qualities, for example, as raw, technical or pharmaceutical grade.
  • Glycerine which is available in the raw grade, usually accrues in the production of biodiesel.
  • vegetable oils and fats in which a glycerol molecule is esterified with three fatty acid molecules, usually after heating with addition of catalyst (NaOH or sodium methoxide) with methanol to fatty acid methyl esters (biodiesel) transesterified.
  • the co-product is glycerin.
  • By-products are sodium salts of fatty acids (soaps).
  • the aqueous mixture of glycerin, soaps, methanol, catalyst and water is usually physically separated from the lipophilic fatty acid methyl ester. Acidification with hydrochloric acid produces fatty acids and sodium chloride. Crude glycerin and fatty acid are generally separated by phase separation. The removal of the methanol is carried out by distillation.
  • Crude glycerol generally has a water content of 5 to 30 wt .-%, usually 10 to 15 wt .-%, a salt content of 0.1 to 10 wt .-%, usually 5 to 7 wt .-%, and a methanol content of less than 1 wt .-%, usually 0.1 to 0.5 wt .-%, on.
  • Technical grade or pharmaceutical grade glycerin is typically purified by distillation in one or more stages to reduce salt content and color number.
  • glycerin is available in various glycerol levels (e.g., 99.8% or 99.5% Nobel's Glycerin).
  • glycerin eg European Pharmacopoeia or European Pharmacopoeia (Ph. Eur.), United States Pharmacopeia (USP), Japanese Pharmacopoeia
  • the glycerol content is usually more than 99%, eg 99.5% or 99.8%.
  • the glycerol used is usually clear and bright and usually has a color number of less than 100 APHA, preferably less than 50 APHA and more preferably less than 20 APHA.
  • the salt content of the glycerol used is usually less than
  • 0.1 wt .-% preferably less than 0.05 wt .-%.
  • the glycerol used may also contain water, the water content should generally not more than 50 wt .-%, preferably less than 20 wt .-% and more preferably less than 5 wt .-% should be.
  • the glycerine may also contain sulfur-containing components.
  • crude glycerol may possibly lead to undesirable deposits in the reactor due to a higher salt content and due to a higher content of by-products lead to a stronger discoloration of the inventive amines. If crude glycerol is to be used in the process, measures may have to be taken, such as a more frequent cleaning of the reactor or a purification of the reaction output in order to obtain a product suitable for the respective application.
  • the aminating agent is selected from the group consisting of ammonia, primary amines and secondary amines.
  • primary or secondary amines can be used as aminating agents.
  • the following mono- and dialkylamines can be used as aminating agents: methylamine, dimethylamine, ethylamine, diethylamine, n-propylamine, di-n-propylamine, iso-propylamine, diisopropylamine, isopropylethylamine, n-butylamine, di-n Butylamine, s-butylamine, di-s-butylamine, iso-butylamine, n-pentylamine, s-pentylamine, iso-pentylamine, n-hexylamine, s-hexylamine, iso-hexylamine, cyclohexylamine, aniline, toluidine, piperidine , Morpholine and pyrrolidine.
  • aminating agents such as ammonia, methylamine or diethylamine, are preferably used.
  • Ammonia is particularly preferably used as the aminating agent.
  • water can be added to the process.
  • the catalysts used in the process of the invention contain one or more metals of groups 8 and / or 9 and / or 10 and / or 1 1 of the Periodic Table of the Elements (Periodic Table in the ILJPAC version of 22.06.2007, http: //www.iupac .org / reports / periodic_table / l UPAC_Periodic_Table-22Jun07b.pdf).
  • metals are Cu, Co, Ni and / or Fe, as well as noble metals such as Rh, Ir, Ru, Pt, Pd, and Re.
  • the above-mentioned metals can be used in the form of metal nets or lattices.
  • the metals are used in the form of sponge or skeletal catalysts according to Raney in the process according to the invention. Particular preference is given to using nickel and / or cobalt catalysts according to Raney.
  • Raney nickel or cobalt catalysts are usually prepared by treating an aluminum-nickel alloy or an aluminum-cobalt alloy with concentrated sodium hydroxide solution, leaching the aluminum and forming a metallic nickel or cobalt sponge.
  • the production of catalysts according to Raney is described, for example, in the Handbook of Heterogeneous Catalysis (MS Wainright in G. Ertl, H. Knoeginger, J. Weitkamp (eds.), Handbook of Heterogeneous Catalysis, Vol. 1, Wiley-VCH, Weinheim, Germany 1997, page 64 ff.).
  • Such catalysts are available, for example, as Raney® catalysts from Grace or as Sponge Metal® catalysts from Johnson Matthey.
  • the catalysts which can be used in the process according to the invention can also be prepared by reduction of so-called catalyst precursors.
  • the catalyst precursor contains an active material which contains one or more catalytically active components and optionally a carrier material.
  • the catalytically active components are oxygen-containing compounds of the metals of groups 8 and / or 9 and / or 10 and / or 1 of the Periodic Table of the Elements (Periodic Table in the ILJPAC version of June 22, 2007), for example their metal oxides or hydroxides, (possibly examples), such as CoO, NiO, Mn3Ü4, CuO, RuO (OH) x and / or their mixed oxides, such as LJCOO2.
  • the mass of the active mass is the sum of the mass of the carrier material and the mass of the catalytically active components.
  • the catalyst precursors used in the process may contain, in addition to the active material, deformation agents such as graphite, stearic acid, phosphoric acid or other processing aids.
  • the catalyst precursors used in the process may further contain one or more dopants (oxidation state 0) or their inorganic or organic compounds selected from groups 1 to 14 of the periodic table.
  • dopants oxygen state 0
  • elements or their compounds are: transition metals, such as Mn or manganese oxides, Re or rhenium oxides, Cr or chromium oxides, Mo or molybdenum oxides, W or tungsten oxides, Ta or tantalum oxides, Nb or niobium oxides or niobium xalate, V or vanadium oxides or vanadyl pyrophosphate, zinc or zinc oxides, silver or silver oxides, lanthanides, such as Ce or CeO 2 or Pr or Pr 2 O 3 , alkali metal oxides, such as K 2 O, alkali metal carbonates, such as Na 2 CO 3 and K 2 CO 3 , alkaline earth metal oxides , such as SrO, alkaline earth metal carbonates, such as MgC ⁇
  • the catalyst precursors are preferably used in the form of catalyst precursors which are only composed of catalytically active composition, if appropriate a molding assistant (such as graphite or stearic acid), if the catalyst is used as a molding, and optionally one or more doping elements exist, but in addition contain no further catalytically active impurities.
  • a molding assistant such as graphite or stearic acid
  • the carrier material is considered to belong to the catalytically active mass.
  • compositions given below relate to the composition of the catalyst precursor after its last heat treatment, which is generally a calcination, and before its reduction with hydrogen.
  • the proportion of the active material based on the total mass of the catalyst precursor is usually 70 wt .-% or more, preferably 80 to 100 wt .-%, particularly preferably 90 to 99 wt .-%, in particular 92 to 98 wt .-%.
  • the active mass of the catalyst precursor contains no carrier material.
  • the active material of catalyst precursors containing no support material preferably contains one or more active components selected from the group consisting of CoO, NiO, Mn 3 O 4 , CuO, RuO (OH) x and LiCoO 2 .
  • the active mass of catalyst precursors containing no support material contains NiO and / or CoO.
  • Such catalyst precursors are for example
  • the active composition contains carrier material in addition to the catalytically active components.
  • Catalyst precursors containing support material may contain one or more catalytically active components, preferably CoO, NiO, M ⁇ O 4 , CuO and / or oxygen-containing compounds of Rh, Ru and / or Ir. More preferably, the active material of catalyst precursors containing support material contains NiO and / or CoO.
  • Preferred carrier materials are 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, etc., and mixtures of these carrier materials used.
  • the amount of support material on the active mass can vary over a wide range depending on the manufacturing method chosen.
  • the proportion of support material in the active composition is generally more than 50% by weight, preferably more than 75% by weight, and more preferably more than 85% by weight.
  • the proportion of support material in the active material is in usually in the range of 10 to 90 wt .-%, preferably in the range of 15 to 80 wt .-% and particularly preferably in the range of 20 to 70 wt .-%.
  • Such catalyst precursors obtained by precipitation reactions are, for example
  • Catalysts disclosed in EP-A-696572 whose catalytically active composition prior to reduction with hydrogen contains 20 to 85% by weight ZrO 2 , 1 to 30% by weight oxygen-containing compounds of copper, calculated as CuO, 30 to 70% by weight.
  • % oxygen-containing compounds of nickel, calculated as NiO, 0.1 to 5 wt .-% oxygen-containing compounds of molybdenum, calculated as Mo ⁇ 3, and 0 to 10 wt .-% oxygen-containing compounds of aluminum and / or manganese, calculated as AI2O3 or MnO 2 contains, for example, the in loc. cit, page 8, disclosed catalyst having the composition 31, 5 wt .-% ZrO 2 , 50 wt .-% NiO, 17 wt .-% CuO and 1, 5 wt .-% MoO 3 ,
  • Catalysts disclosed in EP-A-963 975 whose catalytically active composition prior to reduction with hydrogen contains from 22 to 40% by weight ZrO 2 , from 1 to 30% by weight of oxygen-containing compounds of copper, calculated as CuO, from 15 to 50% by weight.
  • copper-containing catalysts disclosed in DE-A-2445303 eg the copper-containing precipitation catalyst disclosed in Example 1, which is prepared by treating a solution of copper nitrate and aluminum nitrate with sodium bicarbonate followed by washing, drying and tempering of the precipitate and a composition of about 53 wt % Of CuO and about 47% by weight of Al 2 O 3 , or
  • WO 96/36589 disclosed catalysts, in particular those containing Ir, Ru and / or Rh and as a carrier material activated carbon.
  • the catalyst precursors can be prepared by known methods, for example by precipitation, precipitation, impregnation.
  • catalyst precursors are used in the process of the invention, which are prepared by impregnation (impregnation) of support materials (impregnated catalyst precursor).
  • the carrier materials used in the impregnation can be used, for example, in the form of powders or shaped articles, such as strands, tablets, spheres or rings.
  • suitable carrier material is preferably obtained by spray drying.
  • Suitable support materials are, 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.
  • the impregnation of the abovementioned support materials can be carried out by the usual 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.
  • metal salts are usually water-soluble metal salts, such as the nitrates, acetates or chlorides of the above elements into consideration.
  • the impregnated support material is usually dried and optionally calcined.
  • the impregnation can also be carried out by the so-called "incipient wetness method", in which the support material is moistened to the maximum saturation with the impregnation solution in accordance with its water absorption capacity.
  • the impregnation can also be done in supernatant solution.
  • multistage impregnation methods it is expedient to dry between individual impregnation steps and, if appropriate, to calcine.
  • the multi-step impregnation is advantageous to apply when the carrier material is to be applied in a larger amount with metal salts.
  • the impregnation can take place simultaneously with all metal salts or in any order of the individual metal salts in succession.
  • catalyst precursors are prepared via a co-precipitation (mixed precipitation) of all their components.
  • a soluble metal salt of the corresponding metal oxides and optionally a soluble compound of a support material in a liquid in the heat and with stirring are added with a precipitating agent until the precipitation is complete.
  • the liquid used is usually water.
  • the soluble metal salts of the corresponding metal oxides are usually the corresponding nitrates, sulfates, acetates or chlorides of the metals of groups 8 and / or 9 and / or 10 and / or 11 of the Periodic Table of the Elements (Periodic System in the ILJPAC version from 22.06. 2007).
  • Examples of such metals are Cu, Co, Ni and / or Fe, as well as noble metals such as Rh, Ir, Ru, Pt, Pd, and Re.
  • Water-soluble compounds of a carrier material are generally water-soluble compounds of Al, Zr, Si, etc., for example the water-soluble nitrates, sulfates, acetates or chlorides of these elements.
  • Catalyst precursors can be further prepared by precipitation.
  • Precipitation is understood as meaning a preparation method in which a sparingly soluble or insoluble carrier material is suspended in a liquid and subsequently soluble metal salts of the corresponding metal oxides are added, which are then precipitated onto the suspended carrier by addition of a precipitant (for example described in EP-A2- 1 106 600, page 4, and AB Stiles, Catalyst Manufacture, Marcel Dekker, Inc., 1983, page 15).
  • heavy or insoluble support materials are carbon compounds, such as graphite, carbon black and / or activated carbon, aluminum oxide (gamma, delta, tetra, alpha, kappa, chi or mixtures thereof), silica, zirconium dioxide, zeolites, aluminosilicates or their mixtures into consideration.
  • carbon compounds such as graphite, carbon black and / or activated carbon, aluminum oxide (gamma, delta, tetra, alpha, kappa, chi or mixtures thereof), silica, zirconium dioxide, zeolites, aluminosilicates or their mixtures into consideration.
  • the carrier material is usually present as a powder or grit.
  • water As a liquid in which the carrier material is suspended, water is usually used.
  • soluble metal salts of the corresponding metal oxides are usually the corresponding nitrates, sulfates, acetates or chlorides of the metals of groups 8 and / or 9 and / or 10 and / or 11 of the Periodic Table of the Elements (Periodic Table in the ILJPAC version of 22.06.2007).
  • metals are Cu, Co, Ni and / or Fe, as well as noble metals such as Rh, Ir, Ru, Pt, Pd and Re.
  • the type of soluble metal salts used is generally not critical. Since it depends primarily on the water solubility of the salts in this approach, a criterion is their required for the preparation of these relatively highly concentrated salt solutions, good water solubility. It is taken for granted that in the selection of the salts of the individual components, of course, only salts with such anions are chosen which do not lead to disturbances, either by causing undesired precipitation reactions or by complicating or preventing precipitation by complex formation .
  • the soluble compounds are precipitated by addition of a precipitant as sparingly or insoluble, basic salts.
  • the precipitants used are preferably bases, in particular mineral bases, such as alkali metal bases. Examples of precipitants are sodium carbonate, sodium hydroxide, potassium carbonate or potassium hydroxide.
  • ammonium salts for example ammonium halides, ammonium carbonate, ammonium hydroxide or ammonium carboxylates.
  • the precipitation reactions can, for example, at temperatures of 20 to 100 0 C, especially 30 to 90 0 C, in particular at 50 to 70 0 C, are performed.
  • the precipitates obtained in the precipitation reactions are generally chemically non-uniform and generally contain mixtures of the oxides, oxide hydrates, hydroxides, carbonates and / or bicarbonates of the metals used. It may prove beneficial for the filterability of the precipitates when they are aged, i. if left for some time after precipitation, possibly in heat or by passing air through it.
  • the precipitates obtained by these precipitation processes are usually processed by washing, drying, calcining and conditioning.
  • the calcination is carried out generally at temperatures between 300 and 800 0 C, preferably 400 to 600 ° C, in particular at 450 to 550 ° C.
  • the catalyst precursors obtained by precipitation reactions are usually conditioned.
  • the conditioning can be carried out, for example, by adjusting the precipitation catalyst by grinding to a specific particle size. After milling, the catalyst precursor obtained by precipitation reactions can be mixed with molding assistants, such as graphite or stearic acid, and further processed to give moldings.
  • molding assistants such as graphite or stearic acid
  • After conditioning or shaping is usually a tempering.
  • the temperatures during the heat treatment usually correspond to the temperatures during the calcination.
  • the catalyst precursors obtained by precipitation reactions contain the catalytically active components in the form of a mixture of their oxygenated compounds, i. in particular as oxides, mixed oxides and / or hydroxides.
  • the catalyst precursors produced in this way can be stored as such.
  • catalyst precursors obtained by impregnation or precipitation as described above are generally prereduced by treatment with hydrogen after calcination.
  • the catalyst precursors are generally first exposed at 150 to 200 0 C over a period of 12 to 20 hours of a nitrogen-hydrogen atmosphere and then treated for up to about 24 hours at 200 to 400 0 C in a hydrogen atmosphere.
  • some of the oxygen-containing metal compounds present in the catalyst precursors are reduced to the corresponding metals so that they coexist with the various oxygen compounds in the active form of the catalyst.
  • the pre-reduction of the catalyst precursor is carried out in the same reactor in which the hydrogenating amination of glycerol is subsequently carried out.
  • the catalyst thus formed may be handled and stored after prereduction 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 employed.
  • the catalyst can also be passivated with a nitrogen-containing gas stream such as air or a mixture of air with nitrogen after prereduction, ie provided with a protective oxide layer.
  • a nitrogen-containing gas stream such as air or a mixture of air with nitrogen after prereduction, ie provided with a protective oxide layer.
  • the storage of the catalysts, obtained by prereduction of catalyst precursors, under inert substances or the passivation of the catalyst make possible uncomplicated and safe handling and storage of the catalyst. If appropriate, the catalyst must then be freed from the inert liquid before the actual reaction or the passivation layer z. B. be lifted by treatment with hydrogen or a gas containing hydrogen.
  • the catalyst can be freed from the inert liquid or passivation layer before the beginning of the hydroamination. This is done, for example, by treating the catalyst with hydrogen or a gas containing hydrogen. Preferably, the hydroamination is carried out directly after the treatment of the catalyst in the same reactor, in which the treatment of the catalyst with hydrogen or a hydrogen-containing gas was carried out.
  • catalyst precursors can also be used without prereduction in the process, wherein they are then reduced under the conditions of the hydrogenating amination by the hydrogen present in the reactor, wherein the catalyst usually forms in situ.
  • the hydrogenating amination can be carried out, for example, in a stirred autoclave, a bubble column, a circulation reactor such as a jet loop or a fixed bed reactor.
  • the process according to the invention can be carried out batchwise or, preferably, continuously.
  • the hydrogenating amination of glycerol can be carried out in the liquid phase or in the gas phase.
  • the hydrogenating amination of glycerol is preferably carried out in the liquid phase.
  • a suspension of glycerol and catalyst is usually initially charged in the reactor.
  • the suspension of glycerol and catalyst with hydrogen and the aminating agent usually has to be well mixed, for example by a turbine stirrer in an autoclave.
  • the suspended catalyst material can be introduced by conventional techniques and separated again (sedimentation, centrifugation, cake filtration, cross-flow filtration).
  • the catalyst can be used one or more times.
  • the catalyst concentration is advantageously 0.1 to 50 wt .-%, preferably 0.5 to 40 wt .-%, particularly preferably 1 to 30 wt .-%, in particular 5 to 20 wt .-%, each based on the total weight of Suspension consisting of glycerol and catalyst.
  • the middle catalyst particle Ankle size is advantageously in the range of 0.001 to 1 mm, preferably in the range of 0.005 to 0.5 mm, in particular 0.01 to 0.25 mm.
  • a dilution of the educts with a suitable inert solvent, in which glycerol has a good solubility, such as tetrahydrofuran, dioxane, N-methylpyrrolidone, take place.
  • glycerol including hydrogen and aminating agent (ammonia or amine)
  • aminating agent ammonia or amine
  • the catalyst loading is generally in the range of 0.05 to 5, preferably 0.1 to 2, more preferably 0.2 to 0.6 kg of glycerol per liter of catalyst (bulk volume) and hour.
  • the pressure is generally from 5 to 40 MPa (50-400 bar), preferably 10 to 30 MPa, more preferably 15 to 25 MPa.
  • the temperature is generally from 100 to 400 0 C, preferably 150 to 300 0 C, particularly preferably 180 to 250 ° C.
  • a dilution of the starting materials with a suitable inert solvent, in which glycerol has a good solubility, such as tetrahydrofuran, dioxane, N-methylpyrrolidone, take place.
  • the gaseous educts (glycerol plus aminating agent) are usually passed over the catalyst in a gas stream of sufficient size for evaporation, in the presence of hydrogen.
  • the pressure is generally from 0.01 to 40 MPa (0.1-400 bar), preferably 0.1 to 10 MPa, more preferably 0.1 to 5 MPa.
  • the temperature is generally from 100 to 400 0 C, preferably 150 to 300 0 C, particularly preferably 180 to 250 ° C.
  • the aminating agent is preferably used in the 0.90 to 250-fold molar amount, particularly preferably in the 1, 0 to 100-fold molar amount, in particular in the 1, 0 to 10-fold molar amount, in each case based on glycerol ,
  • ammonia is generally used with a 1.5 to 250 times, preferably 2 to 100 times, in particular 2 to 10 times, the molar excess per mole of glycerol. Higher excesses of both ammonia and primary or secondary amines are possible.
  • water can be used in the process according to the invention.
  • Water can be supplied to the process in the form of an aqueous glycerol solution together with glycerol, for example, but it can also be fed separately from the other starting materials to the reactor.
  • the molar ratio of water to glycerol is less than 10: 1, preferably less than 8: 1.
  • no additional water is supplied to the process.
  • the hydrogen is generally added to the reaction in an amount of from 5 to 400 l, preferably in an amount of from 150 to 600 l, per mole of glycerol, the liter data being in each case converted to standard conditions (S.T.P.).
  • the pressure in the reaction vessel which results from the sum of the partial pressures of the aminating agent, of glycerol and the reaction products formed and optionally of the solvent used at the indicated temperatures, is expediently increased to the desired reaction pressure by pressing on hydrogen.
  • the excess aminating agent can be recycled together with the hydrogen.
  • the catalyst is arranged as a fixed bed, it may be advantageous for the selectivity of the reaction to see the shaped catalyst bodies in the reactor with inert fillers to be mixed, so to speak to "dilute" them.
  • the proportion of fillers in such catalyst preparations may be 20 to 80, especially 30 to 60 and especially 40 to 50 parts by volume.
  • reaction water formed in the course of the reaction in each case one mole per mole of reacted alcohol group
  • the reaction water formed in the course of the reaction generally does not interfere with the degree of conversion, the reaction rate, the selectivity and the catalyst lifetime and is therefore expediently removed only during the work-up of the reaction product from this, z. B. distillative or extractive.
  • Amines of glycerine, hydrogen and an aminating agent selected from the group consisting of ammonia, primary and secondary amine can be prepared by the process according to the invention.
  • reaction discharge is generally carried out containing
  • glycerol-analogous special amines is understood as meaning those amines which are characterized in that at least one hydroxyl group of glycerol has been substituted by a primary amino group, a secondary amino group or a tertiary amino group.
  • ammonia is used as the aminating agent, a hydroxyl group of glycerin is substituted by a primary amino group.
  • a primary amine for example, methylamine
  • a secondary amino group for example, aminomethyl
  • a secondary amine for example, dimethylamine
  • a hydroxyl group of glycerine is substituted by a tertiary amino group, for example, aminodimethyl.
  • the composition of the reaction effluent can be influenced by the glycerol conversion, the reaction temperature and the composition of the catalyst.
  • the composition of the catalyst used can influence the composition of the amines in the reaction effluent.
  • the catalyst used is a catalyst which contains Ni and / or Co, for example a nickel or cobalt catalyst according to Raney or a catalyst which has been obtained by reduction of a catalyst precursor and whose active material before reduction with hydrogen as the catalytic active component NiO and / or CoO.
  • Such catalysts generally have high activity and in particular favor the formation of alkanolamines, diamines, glycerol-based specialty amines and / or piperazine derivatives.
  • the presence of the catalytically active component NiO promotes the formation of glycerol-analogous special amines.
  • An embodiment in which the catalyst used is a Cu-containing catalyst is also preferred.
  • the use of Cu-containing catalysts usually leads to a higher proportion of Piperazinderivaten and / or diamines in the reaction.
  • catalysts which contain one or more metals of the 5th period of the groups 8 and / or 9 and / or 10 and / or 11 of the Periodic Table of the Elements, preferably Ru and / or Rh, in the inventive Method used.
  • the use of such catalysts generally leads preferably to the formation of monoamines, such as methylamine, ethylamine and / or iso-propylamine when using ammonia as the aminating agent.
  • sponge catalysts according to Raney with Ni or Co as active metal are used in the process according to the invention.
  • Raney sponge catalysts with Ni or Co as the active metal generally favor the formation of aeyclic diamines or glycerol-analogous special amines. Since these catalysts have a particularly high activity, even at low temperatures or short reaction times, a high yield of glycerol-analogous special mines or industrially important amines such as propanediamine and ethylenediamine is obtained when using ammonia as the aminating agent.
  • a further preferred embodiment relates to the use of catalysts which contain Ir in the process according to the invention. Catalysts which contain Ir usually lead to a higher proportion of glycerol-analogous special amines.
  • composition of the reaction effluent may be further affected by the glycerin
  • High glycerol conversions for example glycerol conversions of 80% and more, preferably 90% and more, particularly preferably 99% and more, generally favor the formation of reaction effluents with a high proportion of cyclic amines, such as piperazine and / or piperazine derivatives ,
  • Average glycerol conversions for example glycerol conversions of from 30 to 80%, preferably from 40 to 70% and particularly preferably from 50 to 60%, generally favor the formation of glycerol-analogous special amines.
  • the glycerol conversion can be influenced by a number of process parameters, such as pressure, temperature, the molar ratio of aminating agent, in particular ammonia, to glycerol, and the reaction or residence time.
  • High glycerol conversions for example 80 to 100%, can be achieved, for example, by increasing the temperature or increasing the molar ratio of aminating agent, in particular ammonia, to glycerol.
  • high glycerol conversions in a temperature range of usually 200 to 400 0 C, preferably 220 to 350 0 C can be achieved.
  • the molar ratio of aminating agent, especially ammonia, to glycerol to achieve high glycerol conversions is in the range of 5: 1 to 250: 1, preferably 10: 1 to 150: 1.
  • High glycerol conversions are generally achieved at catalyst loadings in the range of 0.05 to 0.6 kg of glycerol per liter of catalyst (bulk volume) and hour, preferably 0.05 to 0.2 per liter of catalyst (bulk volume) and hour. Furthermore, it is possible to effect a high glycerol conversion in a batchwise process by increasing the residence time or by increasing the cata- lator concentration. Usually, high glycerol conversions are added
  • Average glycerol conversions for example 30 to 80%, can be achieved, for example, by reducing the temperature or reducing the molar ratio of ammonia to glycerol.
  • Mean glycerol conversions can be preferably from 150 to 220 0 C, obtained for example in a temperature range of usually 150 to 300 ° C.
  • the molar ratio of aminating agent, in particular ammonia, to glycerol in the achievement of high conversions is in the range of 1: 1 to 100: 1, preferably 2.5: 1 to 50: 1. It is possible to effect a reduction in glycerol conversion in a continuous process by increasing the catalyst loading. Average glycerol conversions are generally achieved at catalyst loadings in the range from 0.1 to 1.2 kg of glycerol per liter of catalyst (bulk volume) and hour, preferably 0.2 to 0.6 per liter of catalyst (bulk volume) and hour.
  • Average glycerol conversions are usually at residence times from 5 to 20 hours, preferably 10 to 16 hours, wherein the residence time depending on the catalyst concentration may also be shorter or longer, in order to achieve an average glycerol conversion.
  • a catalyst containing Ni and / or Co is used and an average glycerol conversion, for example a glycerol conversion of 30 to 80%, preferably 40 to 70% and particularly preferably 50 to 60%, is set.
  • An average glycerol conversion can usually be adjusted as described above.
  • the reaction output obtained by this particular embodiment of the process contains a proportion of glycerol-analogous special amines of generally more than 5% by weight, preferably more than 10% by weight, based on the total mass of the amines formed.
  • the reaction product prepared by this embodiment of the process contains 1,2,3-triaminopropane when ammonia is used as the aminating agent.
  • an Ir-containing catalyst is used and an average glycerol conversion is set.
  • the setting of an average glycerol conversion for example 30 to 80%, can generally be achieved in the manner mentioned above.
  • the reaction product obtained by this particular embodiment of the process contains a proportion of glycerol-analogous special amines of generally more than 5% by weight, preferably more than 10% by weight, based on the total mass of the amines formed.
  • a high glycerol conversion for example more than 80%, preferably more than 90%, particularly preferably more than 99%, is set. High glycerol conversions can be adjusted, for example, as described above.
  • the reaction product obtained by this particular embodiment of the process contains a proportion of piperazine and / or piperazine derivatives of, as a rule more than 10 wt .-%, preferably 20 wt .-% to 80 wt .-% and particularly preferably 30 to 70 wt .-%, based on the total mass of the amines formed.
  • a catalyst containing one or more metals of the 5th period of groups 8 and / or 9 and / or 10 and / or 1 is used and a high glycerol conversion is established.
  • the setting of a high glycerol conversion for example more than 80%, can generally be achieved in the manner mentioned above.
  • the reaction output obtained by this particular embodiment of the process contains a proportion of monoamines of generally more than 30% by weight, based on the total mass of the amines formed.
  • a Ni and / or Co-containing catalyst in a temperature range of 150 to 220 0 C is used.
  • a high glycerol conversion for example more than 80%, preferably more than 90%, particularly preferably more than 99%, is set, for example by reducing the catalyst loading or increasing the residence time.
  • the very particular embodiment differs from the above-mentioned embodiment using Ni and / or Co-containing catalysts with high glycerol conversion in that a high glycerol conversion at temperatures in the range of 150 and 220 0 C instead of 220 bis 350 ° C is set.
  • the catalyst loading is generally in the range of 0.05 to 0.6 kg of glycerol per liter of catalyst (bulk volume) and hour, preferably 0.05 to 0.2 per liter of catalyst (bulk volume) and Hour.
  • a high glycerol conversion can generally be achieved by extending the residence time or by increasing the catalyst concentration.
  • the residence time in this particularly preferred embodiment at a residence time more than 20 hours, preferably more than 24 hours and more preferably more than 30 hours, wherein the residence time depending on the catalyst concentration may also be shorter or longer.
  • the molar ratio of aminating agent, especially ammonia, to glycerine to achieve high glycerol conversions in this particular embodiment is in the range of 5: 1 to 250: 1, preferably 10: 1 to 150: 1.
  • the reaction effluent obtained by this very particular embodiment of the process contains a proportion of diaminopropane, diaminopropanol and triamino Propane of more than 10 wt .-%, preferably 20 wt .-% to 80 wt .-% and particularly preferably 30 to 70 wt .-%, based on the total mass of the amine.
  • the reaction product usually contains the amines prepared according to the invention, as well as water, aminating agent, hydrogen and optionally unreacted glycerol.
  • the excess aminating agent and the hydrogen are removed.
  • the excess aminating agent and the hydrogen are advantageously returned to the reaction zone.
  • reaction effluent is dewatered, since water and amines can form aezetrope, which can complicate the distillative separation of the individual amines of the reaction mixture.
  • the dehydration of the aqueous reaction discharge is usually carried out by contacting the aqueous reaction effluent with sodium hydroxide solution.
  • concentration of the sodium hydroxide solution is usually 20 to 80%, preferably 30 to 70% and particularly preferably 40 to 60%.
  • the volume ratio of added sodium hydroxide solution and the reaction output is usually between 0.5: 1 to 2: 1, preferably 1: 1.
  • the contacting of the reaction output with sodium hydroxide solution can be effected by feeding the sodium hydroxide solution in the reaction reactor in which the hydrogenating amination of glycerol has previously been carried out.
  • the sodium hydroxide solution can be added as a continuous stream at the reactor outlet.
  • it can also be brought into contact in a distillation column in countercurrent with the vaporous reaction discharge in the sense of an extractive distillation. Processes for extractive distillation are described, for example, in GB-A-1, 1, 02,370 or EP-A-1312600.
  • reaction effluent is dewatered, for example, when an average glycerol conversion is set, since glycerol usually together with the aqueous phase of the amines formed usually can be completely or almost completely separated.
  • the separation of the reaction product can be carried out by distillation or rectification, liquid extraction or crystallization, wherein the separation can be carried out in one or more stages, wherein the number of stages is usually dependent on the number of components present in the reaction.
  • the reaction effluent can be separated into fractions containing a mixture of different amine components or into fractions containing only one amine component.
  • a separation into fractions containing more than one amine component may be made first. These fractions can subsequently be separated into the individual compounds or components, for example by fine distillation.
  • Unreacted glycerine can be recycled to the process.
  • fractions obtained in the work-up of the reaction effluent, containing one or more amines can be used, for example, as additives in concrete and / or cement production.
  • Such fractions contain for example: 0 to 5 wt .-% diamines, such as 1, 2-diaminopropane;
  • piperazine derivatives such as 2-methylpiperazine, 2,5-bis (aminomethyl) piperazine, 3,5-bis (aminomethyl) piperazine, 2-aminomethyl-6-methylpiperazine, 3 Aminomethyl-5-methylpiperazine and / or 3-aminomethyl-6-methylpiperazine; 10 to 30 wt .-% glycerol analog special amines such as 1, 2,3-triaminopropane, 1, 2-diamino-propan-3-ol and / or 1, 3-diamino-propan-2-ol and 20 to 45 wt. -% glycerin.
  • piperazine derivatives such as 2-methylpiperazine, 2,5-bis (aminomethyl) piperazine, 3,5-bis (aminomethyl) piperazine, 2-aminomethyl-6-methylpiperazine, 3 Aminomethyl-5-methylpiperazine and / or 3-aminomethyl-6-methylpiperazine; 10 to 30 wt .-%
  • such a fraction may contain 15 to 30% by weight of water and further components, such as monoamines, diamines, piperazine, piperazine derivatives and / or alkanolamines.
  • the amines according to the invention such as monoamines selected from the group consisting of methylamine, ethylamine, i-propylamine and n-propylamine, or diamines such as ethylenediamine, 1, 2-propanediamine and 1, 3-propanediamine, or alkanolamines, such as monoethanolamine, 2- Aminopropan-1-ol and 1-aminopropan-2-ol, or glycerol-analog special amines such as 1, 2,3-triaminopropane, 1, 3-diaminopropan-2-ol, 1, 2-diaminopropan-3-ol, 1-aminopropanediol and 2-aminopropanediol, or piperazine, or piperazine derivatives, such as 2-methylpiperazine, 2,6-dimethylpiperazine, 2,5-dimethylpiperazine, 2,5-bis (aminomethyl) -piperazine, 2,6-bis (aminomethyl
  • 1,2,3-Triaminopropane is preferably obtained by hydrogenating amination of glycerol with ammonia using an Ir-containing catalyst or a Ni and / or cobalt-containing catalyst at average glycerol conversions. Average glycerol conversions can be adjusted in the manner described above.
  • 1,2,3-triaminopropane is obtained by using a Ni and / or Co-containing catalyst at high glycerol conversions in a temperature range of 150 to 220 0 C, as described above.
  • 2-Aminomethyl-6-methylpiperazine, 2,5-bis (aminomethyl) -piperazine or 2,6-bis (amino-methyl) -piperazine are preferably prepared by hydrogenating amination of glycerol with ammonia using a Ni and / or cobalt-containing catalyst or a Cu-containing catalyst at high glycerol conversions. High glycerol conversions can be adjusted in the manner described above.
  • glycerin is used effectively and effectively as a source for the production of amines. There will be a procedure provided that it allows both to obtain important technical amines, as well as special glycerol-based amines and piperazine derivatives in order to optimally utilize the raw material glycerol.
  • the composition of the reaction can be regulated within certain limits in order to respond flexibly to demand and sales fluctuations.
  • amines such as methylamine, ethylamine, i-propylamine or n-propylamine, diamines, such as ethylenediamine, 1,2-propanediamine or 1,3-propanediamine, alkanolamines, such as monoethanolamine, 2-aminopropan-1-ol or 1-aminopropan-2-ol, or piperazine, which were previously prepared from petrochemical starting materials.
  • monoamines such as methylamine, ethylamine, i-propylamine or n-propylamine
  • diamines such as ethylenediamine, 1,2-propanediamine or 1,3-propanediamine
  • alkanolamines such as monoethanolamine, 2-aminopropan-1-ol or 1-aminopropan-2-ol
  • piperazine which were previously prepared from petrochemical starting materials.
  • new special glycerine-based amines will also be obtained.
  • Such amines are characterized in that at least one OH group of the glycerol is substituted by a primary amino group, a secondary amino group or a tertiary amino group, for example 1, 2,3-triaminopropane, 1, 3-diaminopropan-2-ol, 1, 2-diamino-propan-3-ol, 1-aminopropanediol or 2-aminopropanediol.
  • These compounds have a high number of functionalities and can therefore represent important intermediates in the synthesis of organic compounds such as crop protection agents, pharmaceuticals, stabilizers, etc.
  • derivatives of piperazine such as 2-methylpiperazine, 2,6-dimethylpiperazine, 2,5-dimethylpiperazine, 2,5-bis (aminomethyl) piperazine, 2,6-bis (aminomethyl) piperazine, 2-aminomethyl-5-methyl-piperazine or 2-aminomethyl-6-methyl-piperazine obtained, which may also represent important synthetic building blocks.
  • the contents of the compounds by gas chromatography (conditions: capillary column RTX 5 amine 30m, film thickness 1, 5 microns, diameter 0.32 mm, method: 5 min 60 0 C, then at 7 ° C / min heat to 280 0 C and at 280 ° C for 20 minutes) as area percent (F%).
  • area percentages of the signals refer to the total area below the measured signals, with the exception of the water signal.
  • the stated glycerol conversions refer to the determined area percent before the beginning and at the end of the reaction.
  • the preparation was carried out as described in the general procedure.
  • the catalyst used was a Raney nickel catalyst. It was used 22.5 g of water and 90 g of ammonia. The final temperature was 200 ° C. Samples were taken after different reaction times. After 32 hours, the gas chromatographic analysis gave the following composition:
  • Ethylenediamine 8%; 1,2-propylenediamine: 22%; Piperazine: 2%; 2-methylpiperazine: 13%; 2,6-dimethyl-piperazine: 11%; 1,2-diaminopropan-3-ol: 21%; 1, 2,3-triaminopropane: 2%.
  • the Glcyerin conversion was 91%.
  • the preparation was carried out as described in the general procedure.
  • the catalyst used was cobalt according to Raney (Raney® 2724 from Grace Davison). It 1 1, 25 g of water and 90 g of ammonia were used. The final temperature was 200 ° C. Samples were taken after different reaction times.
  • the preparation was carried out as described in the general procedure.
  • the catalyst used was a catalyst obtained by prereduction from a catalyst precursor whose catalytically active material prior to reduction with hydrogen was 13% by weight of Cu, calculated as CuO, 28% by weight of Ni, calculated as NiO, 28% by weight. % Co calculated as CoO and 31% by weight Zr calculated as ZrO 2 .
  • the pre-reduction of the catalyst precursor was carried out for 20 hours at a temperature of 280 0 C under a pure hydrogen atmosphere.
  • Ethylene diamine 1%; 1, 2-propylenediamine: 17%; Piperazine: 6%; 2-methylpiperazine: 37%;
  • the preparation was carried out analogously to Example 3, but the reaction temperature was 240 0 C instead of 200 0 C.
  • the preparation was carried out analogously to Example 3, but the reaction temperature was 190 ° C instead of 200 0 C and the amount of ammonia used 78 g, instead of 90 g.
  • the preparation was carried out as described in the general procedure.
  • the catalyst used was a catalyst obtained by prereduction from a catalyst precursor whose catalytically active material prior to reduction with hydrogen was 50% by weight Ni, calculated as NiO, 18% by weight Cu, calculated as CuO, 2 Wt% Mo calculated as MoO 3 and 30 wt% Zr calculated as ZrO 2.
  • the pre-reduction of the catalyst precursor was carried out for 12 hours at a temperature of 280 0 C under a pure hydrogen atmosphere.
  • Ethylene diamine 5%; 1, 2-propylenediamine: 29%; Piperazine: 1%; 2-methylpiperazine: 9%; 2,6-dimethyl-piperazine: 7%; 1,2-diaminopropan-3-ol: 7%; 1, 2,3-Triaminopropane: 0%
  • the glycerol conversion was about 89%.
  • the preparation was carried out as described in the general procedure.
  • the catalyst used was a catalyst which was obtained by prereduction from a catalyst precursor whose catalytically active material before reduction with hydrogen was 85% by weight of Co, calculated as CoO, and 5% by weight of Mn, calculated as Mn.sub.3 U.sub.4. contained.
  • the pre-reduction of the catalyst precursor was carried out for 12 hours at a temperature of 280 0 C under a pure hydrogen atmosphere. It 1 1, 25 g of water and 90 g of ammonia were used. The final temperature was 200 ° C.
  • the preparation was carried out as described in the general procedure.
  • the catalyst used was a catalyst which was obtained by prereduction from a catalyst precursor whose catalytically active material before reduction with hydrogen was 39% by weight of Cu, calculated as CuO, and 30% by weight of Cr, calculated as Cr.sub.2O.sub.3, contained.
  • the pre-reduction of the catalyst precursor was carried out for 20 hours at a temperature of 280 0 C under a pure hydrogen atmosphere.
  • Ethylene diamine 5%; 1,2-propylenediamine: 30%; Piperazine: 2%; 2-methylpiperazine: 10%; 2,6-dimethyl-piperazine: 15%; 1,2-diaminopropan-3-ol: 4%; 1, 2,3-Triaminopropane: 0%
  • the glycerol conversion was about 83%.
  • the reactor was cooled to RT and slowly decompressed at room temperature.
  • the degassed reactor contents were analyzed.
  • the contents of the compounds were determined by gas chromatography (conditions: capillary column RTX 5 amine 30 m, film thickness 1.5 microns, diameter 0.32 mm, method: 5 min 60 ° C, then at 7 ° C / min heat to 280 ° C. and bake out at 280 ° C. for 20 minutes) as surface percentages (F%).
  • the area percentages of the signals refer to the total area below the measured signals, with the exception of the water signal.
  • the stated glycerol conversions refer to the determined area percent before the beginning and at the end of the reaction.
  • the preparation was carried out as described in the general procedure.
  • the catalyst used was a catalyst which was obtained by prereduction from a catalyst precursor whose catalytically active material before reduction with hydrogen was 13% by weight of Cu, calculated as CuO, 28% by weight of Ni, calculated as NiO, 28 Wt% Co calculated as CoO and 31 wt% Zr calculated as ZrO2.
  • the pre-reduction of the catalyst precursor was carried out for 20 hours at a temperature of 280 0 C under a pure hydrogen atmosphere.
  • the preparation was carried out as described in the general procedure.
  • the catalyst used was a catalyst obtained by prereduction from a catalyst precursor whose catalytically active mass consisted of LiCoO 2.
  • the pre-reduction of the catalyst precursor was carried out for 20 hours at a temperature of 300 0 C under a pure hydrogen atmosphere.
  • the preparation was carried out as described in the general procedure.
  • the catalyst used was a catalyst obtained by prereduction from a catalyst precursor whose catalytically active material consisted of RuO (OH) x .
  • Gas chromatographic analysis showed the following composition: methylamine: 10%; Ethylamine: 16%; iso-propylamine: 12%; n-propylamine: 16%; Piperazine: 0%; 2-methylpiperazine: 0%; 1-aminopropan-2-ol and 2-amino-1-ol: 0%; 1, 2-propanediamine: 0%; 1, 2-Diaminopropan-3-ol: 0%
  • the glycerol conversion was about 100%.
  • Example 14 Example 14:
  • the preparation was carried out as described in the general procedure.
  • the catalyst used was a catalyst containing 5% by weight of iridium on activated carbon.
  • the preparation was carried out as described in the general procedure.
  • the catalyst used was a catalyst containing 5% by weight of rhodium on activated carbon.
  • the catalyst precursor used was a catalyst precursor whose active mass was 50% by weight Ni, calculated as NiO, 18% by weight Cu, calculated as CuO, 2% by weight Mo, calculated as MoO 3, and 30% by weight Zr , calculated as ZrÜ2, contained.
  • the catalyst precursor was heated for 12 hours at a temperature of 280 0 C and a hydrogen feed of 200 Nl / h (Nl: standard liters, h: hour) and then reduced for 24 hours at 280 0 C with a hydrogen feed of 200 Nl / h.
  • Glycerol 99.8% pharmaceutical grade from Cognis
  • ammonia and hydrogen in the amount indicated in Table 1 were continuously passed to the reactor in a trickle-bed procedure.
  • the reactor pressure was 200 bar.
  • the temperature of the heat transfer oil at the reactor outlet is given in Table 1.
  • the structure of the piperazine derivatives separated by gas chromatography was determined by mass spectroscopy:
  • the sequence of the transition products was: ethylenediamine, 1,2-propylenediamine, 1,3-propylenediamine, methylpiperazine, 2,6-dimethylpiperazine, 1,2,3-triaminopropane, 1,2-diaminopropan-3-ol, followed by various Isomers of aminomethyl methyl piperazine. Fine distillation of some fractions (525 g) gave 180 g of 1,2,3-triaminoproane in 92% purity.
  • the catalyst precursor used was a catalyst precursor whose active mass was 13% by weight Cu, calculated as CuO, 28% by weight Ni, calculated as NiO, 28% by weight Co, calculated as CoO and 31% by weight Zr, calculated as ZrO 2 contained.
  • the catalyst precursor was hydrogenated for 12 hours
  • the indicated glycerol conversions refer to the area percentages determined before the beginning and at the end of the reaction and are also given in Table 2.
  • Example 32 A portion of the effluent from Example 32 was used in a distillation apparatus with column (1 m column with a diameter of 50 mm, which was filled with 3 mm V2A mesh rings, the number of theoretical plates was 20.) for 10 hours at a Sump temperature of 120 ° C and normal pressure boiled under reflux. In this case, ammonia was depleted to a residual content of 20 ppm. The water content of the mixture was 23% (Karl Fischer titration). The amine numbers were determined by the usual derivatization method by titration. The primary amine number was 228 mg KOH / g; the secondary amine number 317 mg KOH / g and the tertiary amine number 16 mg KOH / g. This corresponds to a total amine number of 561 mg KOH / g. The mixture was used as additives in cement production.
  • 1,2-PDA 1,2-diaminopropane
  • 2-aminopropanol 2-amino-propan-1-ol
  • 1,2,3 TAP 1,2,3-triaminopropane
  • 1,2DAPO 1,2-diamino-propan-3-ol
  • TAP 1, 2,3-triaminopropane
  • 2DAPO 1, 2-diamino-propan-3-ol

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Abstract

L'invention concerne un procédé servant à produire des amines par réaction de glycérine avec de l'hydrogène et un agent d'amination sélectionné dans le groupe contenant ammoniac, amines primaires et amines secondaires, en présence d'un catalyseur à une température comprise entre 100°C et 400°C et une pression comprise entre 0,01 et 40 MPa (0,1 à 400 bars). On utilise de préférence une glycérine à base de matières premières renouvelables. Le catalyseur contient de préférence un métal, plusieurs métaux ou un ou plusieurs composés oxygénés de métaux des groupes 8, 9, 10 et/ou 11 de la classification périodique des éléments. L'invention concerne également l'utilisation des produits réactionnels en tant qu'adjuvants pour la production de ciment ou de béton, ainsi que dans d'autres domaines d'application. L'invention concerne en outre les composés 1,2,3-triaminopropane, 2-aminométhyl-6-méthylpipérazine, 2,5-bis(aminométhyl)-pipérazine et 2,6-bis(aminométhyl)-pipérazine.
EP08787269A 2007-08-29 2008-08-15 Procédé pour produire des amines à partir de glycérine Withdrawn EP2185499A1 (fr)

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CN104693038B (zh) * 2013-12-06 2017-07-28 中国科学院大连化学物理研究所 一种以丙二醇和液氨为原料制备丙二胺的方法及其装置
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US20100240894A1 (en) 2010-09-23
RU2480449C2 (ru) 2013-04-27
WO2009027248A1 (fr) 2009-03-05
RU2010111554A (ru) 2011-10-10
CN101842345A (zh) 2010-09-22
BRPI0815779A2 (pt) 2015-02-24

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