EP4114820A1 - Verfahren zur alkylierung von aminen - Google Patents

Verfahren zur alkylierung von aminen

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Publication number
EP4114820A1
EP4114820A1 EP20922861.8A EP20922861A EP4114820A1 EP 4114820 A1 EP4114820 A1 EP 4114820A1 EP 20922861 A EP20922861 A EP 20922861A EP 4114820 A1 EP4114820 A1 EP 4114820A1
Authority
EP
European Patent Office
Prior art keywords
general formula
metal
compound
metal element
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.)
Pending
Application number
EP20922861.8A
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English (en)
French (fr)
Other versions
EP4114820A4 (de
Inventor
Fan Jiang
Stephane Streiff
Julien Rabih RACHET
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.)
Specialty Operations France SAS
Original Assignee
Rhodia Operations SAS
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Filing date
Publication date
Application filed by Rhodia Operations SAS filed Critical Rhodia Operations SAS
Publication of EP4114820A1 publication Critical patent/EP4114820A1/de
Publication of EP4114820A4 publication Critical patent/EP4114820A4/de
Pending 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/72—Copper
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/74—Iron group metals
    • B01J23/75—Cobalt
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J25/00—Catalysts of the Raney type
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J25/00—Catalysts of the Raney type
    • B01J25/02—Raney nickel

Definitions

  • the present invention pertains to a method for the alkylation of amines.
  • N, N, N', N”, N”-pentamethyldiethylenetriamine is used in the formation of rigid foam polyurethane.
  • Current technology for PMDTA production relies on the methylation of diethylenetriamine (DETA) in the presence of hydrogen by using formaldehyde as methyl source. This methodology is selective towards PMDTA.
  • formaldehyde CMR compound raises HSE concerns.
  • US Patent No. 5105013 teaches a process for the preparation of permethylated amines, particularly pentamethyldiethylenetriamine, by the reductive methylation of diethylenetriamine in the presence of hydrogen, formaldehyde aqueous solution, a catalyst, and a solvent. The reaction was carried out in two reaction phases and the flow rate of formaldehyde must be well controlled.
  • the present invention therefore pertains to a method for preparing a compound having general formula (I) by reacting a compound having general formula (II) with an alcohol having general formula (III) in the presence of hydrogen and a metal catalyst:
  • - R is an alkyl, alkenyl or alkynyl
  • - n is an integer between 0 and 20
  • - m is an integer between 1 and 3
  • - p is an integer between 0 and 2
  • the method of the invention enables to alkylate amines by using an environmentally friendly alkylation agent.
  • the invention also concerns a mixture comprising:
  • Fig. 1 is an image of temperature-yield curve of reaction of DETA with methanol over Pricat Cu 60/8P of Example 3;
  • Fig. 2 is an image of H 2 pressure-yield curve of reaction of DETA with methanol over Pricat Cu 60/8P of Example 4;
  • Fig. 3 is an image of time-yield curve of reaction of DETA with methanol over Pricat Cu 60/8P of Example 5;
  • Fig. 4 is an image of mass ratio (Cat/DETA) -yield curve of reaction of DETA with methanol over Pricat Cu 60/8P of Example 6;
  • Fig. 5 is an image of concentration (DETA in methanol) -yield curve of reaction of DETA with methanol over Pricat Cu 60/8P of Example 7.
  • Ratios, concentrations, amounts, and other numerical data may be presented herein in a range format. It is to be understood that such a range format is used merely for convenience and brevity and should be interpreted flexibly to include not only the numerical values explicitly recited as the limits of the range, but also all the individual numerical values or sub-ranges encompassed within that range as if each numerical value or sub-range is explicitly recited.
  • the compound having general formula (II) is a compound having general formula (IV) :
  • n is an integer between 0 and 20, preferably between 0 and 9, and more preferably between 0 and 4.
  • the compound having general formula (II) is a compound having general formula (V) :
  • n is an integer between 0 and 20, preferably between 0 and 9, and more preferably between 0 and 4.
  • the compound having general formula (II) is a compound having general formula (VI) :
  • n is an integer between 0 and 20, preferably between 0 and 9, and more preferably between 0 and 4.
  • the compound having general formula (II) can be selected from the group consisting of dimethylenetriamine, diethylenetriamine, dipropylenetriamine, dibutylenetriamine, dipentylenetriamine, dihexylenetriamine, diheptylenetriamine, dioctylenetriamine, dinonylenetriamine, didecylenetriamine, methylenediamine, ethylenediamine, propylenediamine, butylenediamine, pentylenediamine, hexylenediamine, heptylenediamine, octylenediamine, nonylenediamine, and decylenediamine, triaminomethylamine, tris (2-aminoethyl) amine, tris (3-aminopropyl) amine, tris (4-aminobutyl) amine, tris (5-aminopentyl) amine, tris (6-aminohexyl) amine, tris (7-aminoh
  • the compound having general formula (II) can be selected from the group consisting of diethylenetriamine, dipropylenetriamine, dibutylenetriamine, dipentylenetriamine, ethylenediamine, propylenediamine, butylenediamine and pentylenediamine.
  • R may be straight or branched. More preferably, R may be a C 1 -C 10 straight or branched alkyl.
  • Examples of the alcohol having general formula (III) are methanol, ethanol, 1-propanol, 1-butanol, 1-pentanol, 1-hexanol, 1-heptanol, 1-octanol, 1-nonanol, 1-decanol, 2-propanol, 2-butanol and 3-butanol.
  • the alcohol having general formula (III) can be selected from the group consisting of methanol, ethanol, 1-propanol and 2-propanol.
  • the alcohol may comprise traces of corresponding aldehyde and/or carboxylic acid.
  • methanol may comprise traces of formaldehyde and/or formic acid
  • ethanol may comprise traces of acetaldehyde and/or acetic acid
  • propanol may comprise traces of propionaldehyde and/or propanoic acid.
  • the alcohol may contain 0.01-10000 ppm corresponding aldehyde and/or carboxylic acid.
  • Preferred reactions of the present invention are the following:
  • the metal catalyst may comprise at least one metal element in elemental form and/or at least one metal oxide of at least one metal element, wherein the metal element is selected from (i) elements of group IA except hydrogen, (ii) elements of group IIA, (iii) elements of group IIIA, (iv) elements of group IVA except carbon, (v) arsenic, antimony, bismuth, tellurium, polonium and astatine, (vi) elements of groups IB, IIB, IIIB, IVB, VB, VIB, VIIB and VIIIB, (vii) lanthanides and (viii) actinides.
  • the metal element is selected from (i) elements of group IA except hydrogen, (ii) elements of group IIA, (iii) elements of group IIIA, (iv) elements of group IVA except carbon, (v) arsenic, antimony, bismuth, tellurium, polonium and astatine, (vi) elements of groups IB, IIB, IIIB, IVB, VB,
  • the metal catalyst according to present invention can be a supported or unsupported catalyst.
  • the support to the metal catalyst is not particularly limited. It can notably be a metal oxide chosen in the group consisting of aluminum oxide (Al 2 O 3 ) , silicon dioxide (SiO 2 ) , titanium oxide (TiO 2 ) , zirconium dioxide (ZrO 2 ) , calcium oxide (CaO) , magnesium oxide (MgO) , lanthanum oxide (La 2 O 3 ) , niobium dioxide (NbO 2 ) , cerium oxide (CeO 2 ) and mixtures thereof.
  • Al 2 O 3 aluminum oxide
  • SiO 2 silicon dioxide
  • TiO 2 titanium oxide
  • ZrO 2 zirconium dioxide
  • CaO calcium oxide
  • MgO magnesium oxide
  • La 2 O 3 lanthanum oxide
  • NbO 2 niobium dioxide
  • CeO 2 cerium oxide
  • the support can also be a zeolite.
  • Zeolites are substances having a crystalline structure and a unique ability to change ions. People skilled in the art can easily understand how to obtain those zeolites by preparation method reported, such as zeolite L is described in US 4503023 or commercial purchase, such as ZSM available from ZEOLYST.
  • the support of catalyst can even be Kieselguhr, clay or carbon.
  • metals are the elements in the periodic system which are located left to the diagonal extending from boron (atomic number 5) to astatine (atomic number 85) ) .
  • Metals of group IA Li, Na, K, Rb, Cs, Fr are also known as alkali metals and metals of group IIA (Be, Mg, Ca, Sr Ba and Ra) are generally referred to as alkaline earth metals.
  • the metals of group IB, IIB, IIIB, IVB, VB, VIB, VIIB and VIIIB are often referred to as transition metals.
  • This group comprises the elements with atomic number 21 to 30 (Sc to Zn) , 39 to 48 (Y to Cd) , 72 to 80 (Hf to Hg) and 104 to 112 (Hf to Cn) .
  • the lanthanides encompass the metals with atomic number 57 to 71 and the actinides the metals with the atomic number 89 to 103.
  • metalloids are sometimes also referred to as metalloids.
  • the term metalloid is generally designating an element which has properties between those of metals and non-metals. Typically, metalloids have a metallic appearance but are relatively brittle and have a moderate electrical conductivity.
  • the six commonly recognized metalloids are boron, silicon, germanium, arsenic, antimony, and tellurium.
  • Other elements also recognized as metalloids include aluminum, polonium, and astatine. On a standard periodic table all of these elements may be found in a diagonal region of the p-block, extending from boron at one end, to astatine at the other (as indicated above) .
  • the metal element is selected from elements of groups IA, IIA, IIIA, IVA, IB, IIB, IIIB, IVB, VB, VIB, VIIB and VIIIB. More preferably, the metal element is selected from elements of groups IA, IIA, IIIA, IVA, IB, IIB, VIB, VIIB and VIIIB.
  • the metal catalyst comprises two, three, or four metal elements, which are present in elemental form and/or in metal oxide form.
  • Metal oxide compounds comprise typically at least one oxygen atom and at least one metal atom which is chemically bound to the oxygen atom; the electronegativity of the oxygen atom is obviously higher than the electronegativity of the metal atom.
  • the metal oxide compound of the present invention may be a single oxide or a mixed oxide.
  • a single metal oxide is typically composed of one or more metal atom (s) of a same, unique metal element and one or more oxygen atom (s) .
  • the metal atom comprised in the single metal oxide can be notably:
  • Ln a lanthanide Ln, as in CeO 2 and in Ln 2 O 3 , or
  • a mixed metal oxide is typically composed of one or more metal atom (s) of different metal elements and one or more oxygen atom (s) .
  • Many metals can form mixed oxides with one or more other metals.
  • Mixed oxide minerals appear in a great variety in nature and synthetic mixed oxides find use as components of different materials used in advanced technological applications.
  • ZnO Al, ZnO: Cu, ZnO: Ag, ZnO: Ga, ZnO: Mg, ZnO: Cd, ZnO: In, ZnO: Sn, ZnO: Sc, ZnO: Y, ZnO: Co, ZnO: Mn, ZnO: Cr and ZnO: B
  • cuprates superconductors such as YBa 2 Cu 3 O 7-x , Bi 2 Sr 2 CuO 6 , Bi 2 Sr 2 CaCu 2 O 8 , Bi 2 Sr 2 Ca 2 Cu 3 O 6 , Tl 2 Ba 2 CuO 6 , Tl 2 Ba 2 CaCu 2 O 8 , Tl 2 Ba 2 Ca 2 Cu 3 O 10 , TlBa 2 Ca 3 Cu 4 O 11 , HgBa 2 CuO 4 , HgBa 2 CaCu 2 O 6 and HgBa 2 Ca 2 Cu 3 O 8 ,
  • A Ni, Mg, Mn, Fe, Co, Zn, Cu, Ca, Sr, Ba or Pb
  • Ln represents a lanthanide metal
  • perovskites such as LaGaO 3 , Na 1-x Bi x TiO 3 with 0 ⁇ x ⁇ 1,
  • IGZO indium-gallium-zinc oxide
  • ITO indium - mixed oxides of indium and tin, commonly referred to as ITO, which denotes a solid solution of indium (III) oxide (In 2 O 3 ) and tin (IV) oxide (SnO 2 ) , consisting essentially of or consisting of from 80 wt. %up to 95 wt. %of In 2 O 3 and from 5 wt. %to 20 wt. %of SnO 2 , in some cases about 90 wt. %In 2 O 3 and about 10 wt. %SnO 2 ; in particular for organic electronic device applications, ITO has been profitably used in the recent past.
  • the metal catalyst according to the present invention can be Raney catalysts such as Raney nickel, Raney cobalt and Raney copper.
  • the metal catalyst comprises Metal element A and optionally Metal element B, which are present in elemental form and/or in metal oxide form, wherein:
  • Metal element A is at least one metal element selected from elements of groups IB and VIIIB, and
  • Metal element B is at least one metal element selected from the group consisting of Al, Na, Mn, Mg, Si, Zn, Ni, Cr, K, Li, Cs, Be, Ca, Sr, Ba, Sc, Y, Ti, Zr, V, Nb, W, Mo, Tc, Re, Fe, Ru, Co, Ag, Cd, Hg, Ga, Pb, Bi, Ce, and mixtures thereof.
  • Metal element A is Cu or Co and Metal element B is at least one metal element selected from the group consisting of Al, Na, Mn, Mg, Si, Zn, Ni, Cr and mixtures thereof.
  • Metal element A can be supported on a support in this embodiment.
  • Said support can be Al 2 O 3 , SiO 2 , TiO 2 , ZrO 2 , ZnO, MgO, NbO 2 , CeO 2 and mixtures thereof.
  • the weight ratio of Metal element A based on the total weight of the catalyst is from 20 to 100 wt%.
  • the metal catalyst may comprise Metal element A being Cu, and Metal element B being Al, Zn and Na.
  • the weight ratio of Cu based on the total weight of the catalyst is from 35 to 55 wt%.
  • the weight ratio of Al based on the total weight of the catalyst is from 3 to 7 wt%.
  • the weight ratio of Zn based on the total weight of the catalyst is from10 to 30 wt%.
  • the weight ratio of Na based on the total weight of the catalyst is from 0 to 1 wt%.
  • the metal catalyst may comprise Metal element A being Cu, and Metal element B being Al and Mn.
  • the weight ratio of Cu based on the total weight of the catalyst is from 40 to 65 wt%.
  • the weight ratio of Al based on the total weight of the catalyst is from 20 to 40 wt%.
  • the weight ratio of Mn based on the total weight of the catalyst is from 2 to 20 wt%.
  • the metal catalyst may comprise Metal element A being Cu and Metal element B being Si.
  • the weight ratio of Cu based on the total weight of the catalyst is from 85 to 100 wt%.
  • the weight ratio of Si based on the total weight of the catalyst is from 0.005 to 10 wt%.
  • the metal catalyst may comprise Metal element A being Cu, and Metal element B being Mg, Cr and Si.
  • the weight ratio of Cu based on the total weight of the catalyst is from 60 to 90 wt%.
  • the weight ratio of Mg based on the total weight of the catalyst is from 0 to 5 wt%.
  • the weight ratio of Cr based on the total weight of the catalyst is from 0 to 3 wt%.
  • the weight ratio of Si based on the total weight of the catalyst is from 0 to 10 wt%.
  • the metal catalyst may comprise Metal element A being Cu, and Metal element B being Al and Si.
  • the weight ratio of Cu based on the total weight of the catalyst is from 40 to 80 wt%.
  • the weight ratio of Al based on the total weight of the catalyst is from 0 to 6 wt%.
  • the weight ratio of Si based on the total weight of the catalyst is from 0 to 10 wt%
  • the metal catalyst may comprise Metal element A being Cu, and Metal element B being Ni and Si.
  • the weight ratio of Cu based on the total weight of the catalyst is from 45 to 95 wt%.
  • the weight ratio of Ni based on the total weight of the catalyst is from 0 to 10 wt%.
  • the weight ratio of Si based on the total weight of the catalyst is from 0 to 10 wt%.
  • the metal catalyst may comprise Metal element A being Cu, and Metal element B being Cr and Si.
  • the weight ratio of Cu based on the total weight of the catalyst is from 50 to 95 wt%.
  • the weight ratio of Cr based on the total weight of the catalyst is from 0 to 40 wt%.
  • the weight ratio of Si based on the total weight of the catalyst is from 0 to 10 wt%.
  • the metal catalyst according to the present invention can further comprise at least one metal sulphide compound.
  • metal sulphide compounds comprise typically at least one sulphur atom and at least one metal atom which is chemically bound to the sulphur atom; the electronegativity of the sulphur atom is obviously higher than the electronegativity of the metal atom.
  • the (or at least one) metal atom comprised in the metal sulphide compound can be notably:
  • the metal catalyst according to the present invention can further comprise at least one metal carbide compound.
  • Metal carbide compounds comprise typically at least one carbon atom and at least one metal atom which is chemically bound to the carbon atom; the electronegativity of the carbon atom is obviously higher than the electronegativity of the metal atom.
  • the (or at least one) metal atom comprised in the metal carbide compound can be notably:
  • LaC 2 lanthanum percarbide
  • Ln 2 C 3 sesquicarbide, wherein Ln denotes a lanthanide
  • the metal catalyst according to the present invention can further comprise at least one metal nitride compound.
  • Metal nitride compounds comprise typically at least one nitrogen atom and at least one metal atom which is chemically bound to the nitrogen atom; the electronegativity of the nitrogen atom is obviously higher than the electronegativity of the metal atom.
  • the (or at least one) metal atom comprised in the metal nitride compound can be notably:
  • the metal nitride is an oxynitride (i.e. a compound that qualifies as metal nitride compound and as metal oxide compound) . Examples thereof are:
  • TaON tantalum oxynitride
  • perovskite oxynitrides such as CaTaO 2 N, SrTaO 2 N, BaTaO 2 N, LaTaON 2 and BaNbO 2 N, and
  • the metal catalyst is composed of metal element in elemental form and/or metal oxide.
  • the metal catalyst according to the present invention can be obtained by pre-reduction of commercial catalysts, such as T-4489 P, T-8031 P from Süd-Chemie, T-4419 P from Clariant and Pricat CU 60/35 P, Pricat CU 50/8 P, Pricat 60/8 P from Johnson Matthey.
  • commercial catalysts such as T-4489 P, T-8031 P from Süd-Chemie, T-4419 P from Clariant and Pricat CU 60/35 P, Pricat CU 50/8 P, Pricat 60/8 P from Johnson Matthey.
  • the skilled person can pre-reduce the commercial catalysts by some well-known ways.
  • the metal catalyst can be obtained by in situ-reduction. That is to say, the commercial catalysts can be in situ-reduced during the reaction of the compound having general formula (II) with the alcohol having general formula (III) in the presence of hydrogen.
  • the weight ratio of the metal catalyst to the compound having general formula (II) is from 0.1 to 10 and preferably from 0.2 to 2.
  • the weight ratio of the compound having general formula (II) to the alcohol having general formula (III) may be from 0.0001 to 0.1 and preferably from 0.001 to 0.05.
  • the alcohol having general formula (III) is the reactant and also the only solvent of the compound having general formula (II) .
  • the reaction may also be carried out in the presence of a second solvent other than the alcohol having general formula (III) as long as the second solvent does not participate in the reaction in place of the alcohol.
  • solvent examples include water, formaldehyde (traces) , formic acid (traces) , benzene, toluene, dimethyl ether, etc.
  • the concentration of the compound having general formula (II) in the solvent may be from 0.01wt%to 9wt%, preferably from 0.1wt%to 5wt%and more preferably from 0.1wt%to 2.5wt%.
  • reaction of the compound having general formula (II) with the alcohol having general formula (III) is desirably carried out under a hydrogen pressure in a range of 15-70 bar, and more preferably 20-50 bar.
  • hydrogen may be added during the reaction to make up for the consumption or continuously circulated through the reaction zone.
  • the reaction may be carried out in the presence of an inert atmosphere such as N 2 or Ar.
  • the reaction time may be from 4 to 24h and preferably from 10 to 20h.
  • the reaction temperature may be from 140°C to 220°C and preferably from 180°C to 200°C.
  • the invention also concerns a mixture comprising:
  • the mixture may further comprise a second solvent selected from the group consisting of water, formaldehyde, formic acid, benzene, toluene and dimethyl ether.
  • a second solvent selected from the group consisting of water, formaldehyde, formic acid, benzene, toluene and dimethyl ether.
  • the mixture may further comprise a compound having general formula (I) .
  • the compound having general formula (I) , the compound having general formula (II) , the alcohol having general formula (III) , the metal catalyst and the solvent have the same meaning as above defined.
  • a gas mixture consisting of H 2 /Ar or H 2 /N 2 in 1/3 to 1/10 ratio is flew through the tube from one outlet to another which is connected directly to the atmosphere.
  • the tube is weighed with and without catalyst to get the real weight ofthe catalyst.
  • the catalyst is used freshly after reduction, or kept in a glove box filled with argon.
  • the autoclave was well sealed under nitrogen, and purged by hydrogen 10 bar and evacuated for 10 times, finally purged with 30 bar of hydrogen.
  • the sealing ofthe reactor is checked by waiting 1 hour at room temperature without stirring, and if the pressure remains unchanged then the reactor is well-sealed. Then the reactor was stirred with mechanical stirring for 1 hour at ambient temperature to allow the absorption of the hydrogen, followed by heating up to 200°C for 10 hours with 500 rounds/min stirring speed.
  • the reactor was cooled down to ambient temperature and the hydrogen gas was evacuated carefully in fume hood.
  • To the reaction mixture was added internal standard bisphenyl with accurate weight. After complete dissolving of bisphenyl, the liquid was firstly weighed and then filtered and analyzed by GC. The conversion and yields were calculated using internal standard calibration.
  • the autoclave was well sealed under nitrogen, and purged by hydrogen 10 bar and evacuated for 10 times, finally purged with 30 bar of hydrogen.
  • the sealing of the reactor is checked by waiting 1 hour at room temperature without stirring, and if the pressure remains unchanged then the reactor is well-sealed. Then the reactor was stirred with mechanical stirring for 1 hour at ambient temperature to allow the absorption of the hydrogen, followed by heating up to 200°C for 20 hours with 500 rounds/min stirring speed.
  • the reactor was cooled down to ambient temperature and the hydrogen gas was evacuated carefully in fume hood. The liquid was firstly weighed and then filtered and analyzed by GC affording 28%yield of PMDTA.
  • the autoclave was well sealed under nitrogen, and purged by hydrogen 10 bar and evacuated for 10 times, finally purged with 50 bar of hydrogen.
  • the sealing of the reactor is checked by waiting 1 hour at room temperature without stirring, and if the pressure remains unchanged then the reactor is well-sealed. Then the reactor was stirred with mechanical stirring for 1 hour at ambient temperature to allow the absorption of the hydrogen, followed by heating up to the temperatures described in Table 4 for 10 hours with 500 rounds/min stirring speed.
  • the reactor was cooled down to ambient temperature and the hydrogen gas was evacuated carefully in fume hood.
  • To the reaction mixture was added internal standard bisphenyl with accurate weight. After complete dissolving of bisphenyl, the liquid was firstly weighed and then filtered and analyzed by GC. The conversion and yields were calculated using internal standard calibration.
  • the autoclave was well sealed under nitrogen, and purged by hydrogen 10 bar and evacuated for 10 times, finally purged with hydrogen till the pressures described in Table 5.
  • the sealing of the reactor is checked by waiting 1 hour at room temperature without stirring, and if the pressure remains unchanged then the reactor is well-sealed. Then the reactor was stirred with mechanical stirring for 1 hour at ambient temperature to allow the absorption of the hydrogen, followed by heating up to 200°C for 10 hours with 500 rounds/min stirring speed.
  • the reactor was cooled down to ambient temperature and the hydrogen gas was evacuated carefully in fume hood.
  • To the reaction mixture was added internal standard bisphenyl with accurate weight. After complete dissolving of bisphenyl, the liquid was firstly weighed and then filtered and analyzed by GC. The conversion and yields were calculated using internal standard calibration.
  • Pre-reduced copper containing catalyst Pricat 60/8P was weighed (0.12g) .
  • a clean autoclave was charged under nitrogen after vacuum&nitrogen exchanges for 3 times, catalyst was transferred into autoclave immediately.
  • the autoclave was well sealed under nitrogen, and purged by hydrogen 10 bar and evacuated for 10 times, finally purged with 50 bar of hydrogen.
  • the sealing of the reactor is checked by waiting 1 hour at room temperature without stirring, and if the pressure remains unchanged then the reactor is well-sealed. Then the reactor was stirred with mechanical stirring for 1 hour at ambient temperature to allow the absorption of the hydrogen, followed by heating up to 200°C for time described in Table 6 with 500 rounds/min stirring speed.
  • the reactor was cooled down to ambient temperature and the hydrogen gas was evacuated carefully in fume hood.
  • To the reaction mixture was added internal standard bisphenyl with accurate weight. After complete dissolving of bisphenyl, the liquid was firstly weighed and then filtered and analyzed by GC. The conversion and yields were calculated using internal standard calibration.
  • Pre-reduced copper containing catalyst Pricat 60/8P was weighed to a certain amount described in Table 7. A clean autoclave was charged under nitrogen after vacuum&nitrogen exchanges for 3 times, catalyst was transferred into autoclave immediately.
  • the autoclave was well sealed under nitrogen, and purged by hydrogen 10 bar and evacuated for 10 times, finally purged with 50 bar of hydrogen.
  • the sealing of the reactor is checked by waiting 1 hour at room temperature without stirring, and if the pressure remains unchanged then the reactor is well-sealed. Then the reactor was stirred with mechanical stirring for 1 hour at ambient temperature to allow the absorption of the hydrogen, followed by heating up to 200°C for 10 hours with 500 rounds/min stirring speed.
  • the reactor was cooled down to ambient temperature and the hydrogen gas was evacuated carefully in fume hood.
  • To the reaction mixture was added internal standard bisphenyl with accurate weight. After complete dissolving of bisphenyl, the liquid was firstly weighed and then filtered and analyzed by GC. The conversion and yields were calculated using internal standard calibration.
  • Pre-reduced copper containing catalyst Pricat 60/8P was weighed (0.13 g) . A clean autoclave was charged under nitrogen after vacuum&nitrogen exchanges for 3 times, catalyst was transferred into autoclave immediately.
  • the autoclave was well sealed under nitrogen, and purged by hydrogen 10 bar and evacuated for 10 times, finally purged with 40 bar of hydrogen.
  • the sealing of the reactor is checked by waiting 1 hour at room temperature without stirring, and if the pressure remains unchanged then the reactor is well-sealed. Then the reactor was stirred with mechanical stirring for 1 hour at ambient temperature to allow the absorption of the hydrogen, followed by heating up to 200°C for 20 hours with 500 rounds/min stirring speed.
  • the reactor was cooled down to ambient temperature and the hydrogen gas was evacuated carefully in fume hood.
  • To the reaction mixture was added internal standard bisphenyl with accurate weight. After complete dissolving of bisphenyl, the liquid was firstly weighed and then filtered and analyzed by GC. The conversion and yields were calculated using internal standard calibration.
  • Pre-reduced copper containing catalyst Pricat 60/8P was weighed (0.12 g) . A clean autoclave was charged under nitrogen after vacuum&nitrogen exchanges for 3 times, catalyst was transferred into autoclave immediately.
  • the autoclave was well sealed under nitrogen, and purged by hydrogen 10 bar and evacuated for 10 times, finally purged with 50 bar of hydrogen.
  • the sealing of the reactor is checked by waiting 1 hour at room temperature without stirring, and ifthe pressure remains unchanged then the reactor is well-sealed. Then the reactor was stirred with mechanical stirring for 1 hour at ambient temperature to allow the absorption of the hydrogen, followed by heating up to 200°C for 10 hours with 500 rounds/min stirring speed.
  • the reactor was cooled down to ambient temperature and the hydrogen gas was evacuated carefully in fume hood.
  • To the reaction mixture was added internal standard bisphenyl with accurate weight. After complete dissolving of bisphenyl, the liquid was firstly weighed and then filtered and analyzed by GC. The conversion and yields were calculated using internal standard calibration. The yield of PMDTA was 68.1%.

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  • Chemical & Material Sciences (AREA)
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  • Chemical Kinetics & Catalysis (AREA)
  • Catalysts (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
EP20922861.8A 2020-03-06 2020-03-06 Verfahren zur alkylierung von aminen Pending EP4114820A4 (de)

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DE102004023529A1 (de) * 2004-05-13 2005-12-08 Basf Ag Verfahren zur kontinuierlichen Herstellung eines Amins
RU2009104740A (ru) * 2006-07-14 2010-08-27 Басф Се (De) Способ получения амина
KR20170083085A (ko) * 2014-11-10 2017-07-17 로디아 오퍼레이션스 직접 아민화 반응에 의한 아민을 형성하는 방법
CN110325520A (zh) * 2016-12-22 2019-10-11 罗地亚经营管理公司 用于生产包含至少两个胺官能团的四氢呋喃化合物的方法

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