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
  • C07C209/44—Preparation of compounds containing amino groups bound to a carbon skeleton by reduction of carboxylic acids or esters thereof in presence of ammonia or amines, or by reduction of nitriles, carboxylic acid amides, imines or imino-ethers
  • C07C209/48—Preparation of compounds containing amino groups bound to a carbon skeleton by reduction of carboxylic acids or esters thereof in presence of ammonia or amines, or by reduction of nitriles, carboxylic acid amides, imines or imino-ethers by reduction of nitriles
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C211/00—Compounds containing amino groups bound to a carbon skeleton
  • C07C211/01—Compounds containing amino groups bound to a carbon skeleton having amino groups bound to acyclic carbon atoms
  • C07C211/26—Compounds containing amino groups bound to a carbon skeleton having amino groups bound to acyclic carbon atoms of an unsaturated carbon skeleton containing at least one six-membered aromatic ring
  • C07C211/27—Compounds containing amino groups bound to a carbon skeleton having amino groups bound to acyclic carbon atoms of an unsaturated carbon skeleton containing at least one six-membered aromatic ring having amino groups linked to the six-membered aromatic ring by saturated carbon chains

Definitions

• the present invention relates to a process for preparing a xylylenediamine by heterogeneously catalyzed hydrogenation of a phthalonitrile.
• Xylylenediamine bis (aminomethyl) benzene
• Xylylenediamine is a useful starting material, e.g. for the synthesis of polyamides, epoxy hardeners or as an intermediate for the preparation of isocyanates.
• xylylenediamine includes the three isomers orffto-xylylenediamine, mefa-xylylenediamine (MXDA) and para-xylylenediamine.
• the phthalonitriles are solids (e.g., isophthalonitrile (IPN) melts at 161 ° C) and have relatively poor solubilities in many organic solvents.
• IPN isophthalonitrile
• US-A-4,482,741 (UOP Inc.) describes the hydrogenation of PDN in the presence of ammonia, a supported Co / Ti catalyst and XDA as a solvent.
• DE-A-21 64 169 (Mitsubishi Gas Chemical Co., Inc.) describes on page 6, last paragraph, the hydrogenation of IPDN to meta-XDA in the presence of a Ni and / or Co catalyst in ammonia as solvent.
• JP-B-46008283 (Toray Industries Inc., ACS Abstract 75: 5222) relates to the hydrogenation of nitriles to primary amines in the presence of lead-containing nickel or cobalt catalysts.
• FR-A1-2 722 784 (Rhone Poulenc) teaches the hydrogenation of dinitriles, such as adiponitrile, to diamines in the presence of nickel catalysts.
• US Pat. No. 3,862,911 (and DE-A-2 260 978) (Rhone Poulenc) describes Ni / Cr / Fe / Al catalysts for the hydrogenation of amines.
• Example 6 B succeeds the hydrogenation of IPDN to MXDA at 85 0 C and 40 bar with a yield of 75%.
• JP-A-2003 327563 discloses a process for the continuous hydrogenation of aromatic dinitriles in ammonia as a solvent in a fixed bed irrigation liquid type reactor in the presence of nickel or cobalt catalysts.
• EP-A1-1 449 825 (Mitsubishi Gas) describes a two-stage preparation of aromatic diamines from aromatic dinitriles, such as IPDN, in the presence of Pd and Ni or Co catalysts.
• EP-A-538 865 (Mitsubishi Gas) describes the use of ruthenium catalysts for the hydrogenation of aromatic dinitriles.
• DD Patent 77,983 (Baltz et al.) Discloses a process for the selective hydrogenation of phthalonitriles in the presence of platinum or palladium-containing catalysts and ammonia.
• US 2,970,170 and GB-B-821 404 (California Research Corp.) relate to a multi-step production process for xylylenediamines starting from the corresponding phthalic acids.
• pressures in the range of 1500 to 10,000 psig (103.4 to 689.5 bar), especially 2000 to 5000 psig (137.9 to 344.7 bar), are taught.
• EP-A1-1 454 895 describes a two-stage process for the hydrogenation of dicyano-benzenes at pressures of 5 to 300 bar, in particular 10 to 200 bar, in the presence of Co, Ni, Pd, Ru or Rh catalysts and optionally in the presence of additives such as alkali metal hydroxides or alkaline earth metal hydroxides.
• US-B1-6,476,267 (Sagami Chemical Research Center) relates to the preparation of aromatic primary amines from nitriles, such as IPDN, in the presence of Ni catalysts and polar solvents and at pressures of 0.1 to 50 kg / cm 2 G (0, 1 to 49 bar), eg ⁇ 19 kg / cm 2 G (18.6 bar).
• GB-B-810 530 Teaches the hydrogenation of iso- or terephthalodinitrile in the presence of ammonia, nickel or cobalt catalysts and aromatic hydrocarbons, water, DMF, methanol or ethanol as solvent.
• EP-A1-913 388 (Air Products) relates to the hydrogenation of nitriles, such as DMAPN, to amines in the presence of Raney cobalt catalysts, LiOH and water and, in the absence of senheit of organic solvents, at pressures in the range of 1 to 300 bar, in particular 5 to 80 bar.
• the present invention has for its object to find an improved economical process for the preparation of a xylylenediamine.
• the method should overcome one or more disadvantages of the prior art methods.
• the xylylenediamine, in particular MXDA, should thereby be obtained in high yield, in particular space-time yield, selectivity, purity and / or color quality.
• a process for the preparation of a xylylenediamine by heterogeneously catalyzed hydrogenation of a phthalonitrile is found, which is characterized in that the hydrogenation in the presence of a cobalt skeleton catalyst, an alkali metal hydroxide and an alcohol and / or ether as a solvent, at an absolute pressure in Range of 1 to 100 bar and a temperature in the range of 40 to 150 0 C is performed.
• the process according to the invention preferably finds application for the preparation of meta-xylylenediamine (MXDA) by hydrogenation of isophthalonitrile (IPDN).
• MXDA meta-xylylenediamine
• IPDN isophthalonitrile
• Advantages of the method according to the invention include, inter alia, due to the possible driving without NH 3 addition and low pressure driving, lower technical equipment and safety expenses and thus lower fixed costs (investment) and variable costs.
• the PDN used in the process as starting material can be synthesized in a previous stage by ammoxidation of the corresponding xylene isomer.
• Such synthesis methods are e.g. in BASF patent applications EP-A-767 165, EP-A-699 476, EP-A-222 249, DE-A-35 40 517 and DE-A-37 00 710, as well as in the above-mentioned.
• the starting material PDN is preferably used in a purity of ⁇ 90% by weight, in particular ⁇ 98% by weight, e.g. 98.2 to 99.9 wt .-%, used. Such purities may e.g. obtained by distillation or rectification of commercially available goods.
• the PDN is dissolved and / or suspended in an alcohol and / or ether.
• the dissolution process at elevated temperature e.g. at 50 to 145 ° C, take place.
• the solvent and / or suspending agent is preferably a Ci -4 alkanol, C 4 - I2 - dialkyl ethers and / or C 3 i 2 -alicyclic ether, in particular a C 4-6 dialkyl ethers and / or C 4-6 - alicyclic ether used.
• THF tetrahydrofuran
• 2-methyl-THF tetrahydropyran
• 1-methyl-THF 2-methyl-THF
• tetrahydropyran 1, 3-dioxepane
• 4-dioxane 1, 3-dioxane and 1, 3-dioxolane.
• Particularly preferred is THF.
• solvent and / or suspending agent it is also possible to use a mixture of two or more of the solvents mentioned.
• a cobalt skeleton catalyst is used according to the invention.
• Typical examples of such catalysts are Raney cobalt catalysts.
• the active catalyst is prepared as a 'metal sponge' from a binary alloy (nickel, iron, cobalt, copper with aluminum or silicon) by dissolving a partner with acid or alkali. Residues of the original alloying partner often act synergistically.
• the catalysts used in the process according to the invention are preferably prepared starting from an alloy of cobalt and a further alloying component which is soluble in alkalis.
• a further alloying component which is soluble in alkalis.
• aluminum is preferably used, but other components such as zinc and silicon or mixtures of such components may be used.
• the soluble alloy component is wholly or partially extracted with alkali, for which example aqueous sodium hydroxide solution can be used.
• alkali for which example aqueous sodium hydroxide solution can be used.
• the catalyst can then z. B. be washed with water or organic solvents.
• promoters are metals of subgroups IB, VIB and / or VIII of the Periodic Table, such as chromium, iron, molybdenum, nickel, copper, etc.
• the activation of the catalysts by leaching the soluble component can either be in the reactor itself or before it is charged to the reactor.
• the preactivated catalysts are sensitive to air and pyrophoric and are therefore usually under a medium such.
• a medium such as water, an organic solvent or a substance which is added in the reaction according to the invention.
• gene solvent, educt, product
• the catalysts can be used as powders for suspension hydrogenations or as shaped articles such as tablets or rods for fixed bed reactors.
• the present invention uses a cobalt skeletal catalyst composed of a Co / Al alloy by leaching with aqueous alkali metal hydroxide solution, e.g. Sodium hydroxide solution, and subsequent washing with water was obtained, and preferably contains as promoters at least one of the elements Fe, Ni, Cr.
• aqueous alkali metal hydroxide solution e.g. Sodium hydroxide solution
• Such catalysts typically still contain cobalt in addition
• Al 1 to 30% by weight Al, especially 2 to 12% by weight Al, very particularly 3 to 6% by weight Al,
• a cobalt skeleton catalyst "Raney 2724" from W.R. Grace & Co. can be used advantageously as catalyst in the process according to the invention.
• Al 2-6 wt.%, Co: ⁇ 86 wt.%, Fe: 0-1 wt.%, Ni: 1-4 wt.%, Cr: 1.5-3.5 wt. -%.
• the PDN is in the presence of alkali metal hydroxide (MOH), especially 0.001 to 5 mol% MOH, more preferably 0.002 to 1.5 mol% MOH, more preferably 0.005 to 1.2 mol% MOH, e.g. 1 mol%, MOH, in each case based on the PDN used reacted.
• MOH alkali metal hydroxide
• the appropriate amount of MOH is an aqueous solution, e.g. as 1 to 25 wt .-% aqueous solution used.
• the catalyst used is previously treated with alkali metal hydroxide (M'OH).
• M'OH alkali metal hydroxide
• This treatment is particularly advantageous when the hydrogenation is carried out in the absence of MOH in the reaction mixture presented.
• This treatment of the catalyst with M'OH can be carried out by methods known to the person skilled in the art, for example by saturating the catalyst with M'OH, for example from 0.01 to 5.0% by weight of M'OH (based on the support material) Presence of a suitable solvent, eg water. (EP-A1-913388, US 6,429,338, US 3,636,108).
• the hydrogenation is particularly preferably and advantageously carried out without the addition of ammonia.
• the reaction temperature of the hydrogenation is in the range of 40 to 150 0 C, preferably 50 to 120 0 C, in particular 60 to 110 ° C, especially 70 and 105 0 C, for example 80 to 100 ° C.
• the absolute pressure in the hydrogenation is in the range from 1 to 100 bar, preferably from 2 to 80 bar, in particular from 5 to 60 bar, very particularly from 10 to 50 bar, e.g. 20 to 40 bar.
• reactors for the process according to the invention for example, conventional high-pressure autoclave can be used.
• the reactors known to the person skilled in the art for this reaction for example fixed-bed or suspension operation
• processes continuously, semibatch, batch
• suspension mode a continuous process or semibatch process is preferred.
• the hydrogenation reactor can be run in straight passage.
• a circulation procedure is possible in which a part of the reactor discharge is returned to the reactor inlet, preferably without prior workup of the circulation stream.
• an optimal dilution of the reaction solution can be achieved, which has a favorable effect on the selectivity.
• the circulation stream can be cooled by means of an external heat exchanger in a simple and cost-effective manner and thus the heat of reaction can be dissipated.
• the reactor can also be operated adiabatically, wherein the temperature rise of the reaction solution can be limited by the cooled circulation stream. Since the reactor does not have to be cooled even then, a simple and cost-effective design is possible.
• An alternative is a cooled tube bundle reactor.
• the XDA corresponding to the PDN used is also presented, e.g. in amounts of 500-1500% by weight, based on the PDN to be used.
• the XDA corresponding to the PDN used is the ortho-XDA, in the case of the meta-dinitrile the MXDA and in the case of the para-dinitrile the para-XDA.
• the conversions of PDN achievable with the method according to the invention are in the range of ⁇ 95%, in particular ⁇ 99%, e.g. ⁇ 96 to 99.9% or 99.5 to 100%, with selectivities (for the formation of XDA) in the range of ⁇ 80%, in particular ⁇ 85%, e.g. 86 to 99.5% or 90 to 99%.
• the solvent-freed reaction product contains, in particular, ⁇ 2% by weight, very particularly ⁇ 1% by weight, e.g. 0 to 0.5% by weight, amidines of formula I and / or higher than the XDA boiling products, e.g. the corresponding (bisaminoalkyl) diarylamine II.
• the isolation of the XDAs can be carried out e.g. by distillation or rectification.
• the autoclave was closed, the mixture made inert, and pressed to 10 bar hydrogen. It was heated to 100 ° C. under autogenous pressure and with stirring (500 rpm). Upon reaching this temperature was pressed to 36 bar of hydrogen and the stirrer speed to 1200 rev / min, increased. Subsequently, a solution of 7.2 g of IPDN in 83 g of THF was pumped in over 5 h, hydrogen being fed continuously (under pressure maintenance at 36 bar). After 5 h, a sample was taken. GC analysis of the samples showed a conversion of 100% and a content of 99.4% after 5 h, which corresponds to a selectivity of 97.7% after deduction of the submitted MXDA. No formation of high boilers was observed. The mixture was held at this temperature for an additional 2 hours without lowering the selectivity.

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• 2005
  • 2005-01-24 DE DE102005003315A patent/DE102005003315A1/de not_active Withdrawn
• 2006
  • 2006-01-19 CN CNA2006800030354A patent/CN101107215A/zh active Pending
  • 2006-01-19 JP JP2007551670A patent/JP2008528459A/ja not_active Withdrawn
  • 2006-01-19 KR KR1020077019237A patent/KR20070107714A/ko not_active Application Discontinuation
  • 2006-01-19 US US11/814,390 patent/US20080214871A1/en not_active Abandoned
  • 2006-01-19 EP EP06707753A patent/EP1843998A1/de not_active Withdrawn
  • 2006-01-19 WO PCT/EP2006/050302 patent/WO2006077233A1/de active Application Filing

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