EP1250301A1 - Procede de preparation de trimethylolalcanes - Google Patents

Procede de preparation de trimethylolalcanes

Info

Publication number
EP1250301A1
EP1250301A1 EP01907401A EP01907401A EP1250301A1 EP 1250301 A1 EP1250301 A1 EP 1250301A1 EP 01907401 A EP01907401 A EP 01907401A EP 01907401 A EP01907401 A EP 01907401A EP 1250301 A1 EP1250301 A1 EP 1250301A1
Authority
EP
European Patent Office
Prior art keywords
formula
formaldehyde
aldehyde
formula iii
dimethylolalkanal
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Withdrawn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
EP01907401A
Other languages
German (de)
English (en)
Inventor
Frank Döbert
Alexander Klausener
Paul Wagner
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.)
Bayer Chemicals AG
Original Assignee
Bayer AG
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Bayer AG filed Critical Bayer AG
Publication of EP1250301A1 publication Critical patent/EP1250301A1/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/132—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group
    • C07C29/136—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH
    • C07C29/14—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH of a —CHO group
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
    • C07C45/61—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reactions not involving the formation of >C = O groups
    • C07C45/67—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reactions not involving the formation of >C = O groups by isomerisation; by change of size of the carbon skeleton
    • C07C45/68—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reactions not involving the formation of >C = O groups by isomerisation; by change of size of the carbon skeleton by increase in the number of carbon atoms
    • C07C45/72—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reactions not involving the formation of >C = O groups by isomerisation; by change of size of the carbon skeleton by increase in the number of carbon atoms by reaction of compounds containing >C = O groups with the same or other compounds containing >C = O groups
    • C07C45/75—Reactions with formaldehyde

Definitions

  • the present invention relates to a process for the preparation of trimethylolalkanes, in particular trimethylolpropane, in high purity and with high yields while simultaneously obtaining calcium formate (Ca (OOCH) 2 ).
  • Trimethylolpropane is used in the production of paint resins, powder coatings, foams and polyesters.
  • Calcium formate is used commercially, for example, in the following areas: additive for animal nutrition, use in the building materials industry, production of formic acid, auxiliary in the leather industry, auxiliary agents in the production of glossy papers, treatment of washing water in the flue gas desulfurization and auxiliary agents in ensiling.
  • TMP trimethylolpropane
  • Amounts of a base for example calcium hydroxide is used, in the final step the formation of trimethylolpropane takes place with the simultaneous release of calcium formate.
  • the process is carried out in one stage, which has the disadvantage that the individual reaction steps, ie the preparation of 2,2-dimethylolbutanal and its conversion to trimethylolpropane, cannot be optimized separately. This manifests itself in the formation of undesirable by-products and in an unsatisfactory yield with regard to the n-butyraldehyde used.
  • two-stage processes have been developed, in a first step 2,2-dimethylolbutanal is first prepared from n-butyraldehyde and formaldehyde and this is then hydrogenated in a second step.
  • DE-A 25 07 461 describes, for example, a two-stage process according to which 2,2-dimethylol butanal is obtained from n-butyraldehyde and formaldehyde in the presence of catalytic amounts of a tertiary trialkylamine which carries at least one branched alkyl radical, which are then subjected to a hydrogenation can.
  • the yield of trimethylolpropane can be significantly increased if, in a first step, the production of 2,2-dimethylolbutanal by condensation of n- Butyraldehyde and formaldehyde in
  • EP-A 860 419 also suggests the production of 2,2-dimethylolbutanal from n-butyraldehyde and formaldehyde, i.e. to carry out the first step of the production of trimethylolpropane in several stages, the actual conversion taking place in the first stage and the 2-ethyl acrolein obtained as a by-product being reacted with further formaldehyde in the second stage.
  • Dimethylol butanal can be hydrogenated to trimethylol propane in a second step.
  • 2,2-dimethylol butanal Before the hydrogenation step, 2,2-dimethylol butanal must be largely free of unreacted starting material, in particular formaldehyde and basic constituents, so that the desired high yields of trimethylol propane can be achieved.
  • the object of the present invention was to provide a process for the preparation of trimethylolalkanes in high yields with respect to the starting materials used, which allows the simultaneous production of calcium formate.
  • R represents methylol, C i -C 1 alkyl, C 6 -C 0 aryl or C 7 -C 22 aralkyl
  • R has the meaning given above, found, which is characterized in that in a first step an aldehyde of the formula II and formaldehyde in the presence of a base to give a 2,2-dimethylolalkanal of the formula III
  • R in the formulas I, II and III represents methylol, C 1 -C 1 -alkyl, such as, for example, methyl, ethyl, propyl, butyl, pentyl, hexyl, isopropyl, isobutyl and tert-butyl, C 6 - cio-aryl, such as phenyl and naphthyl or C 7 -C 22 aralkyl, such as benzyl.
  • R is preferably methylol or C 1 -C 6 -alkyl and particularly preferably methylol or C 1 -C 6 -alkyl.
  • R very particularly preferably represents ethyl.
  • the process according to the invention separates the production of the intermediate 2,2-dimethylolalkanal from the subsequent step, the production of trimethylolalkane, both in terms of process technology and in terms of space. This allows the two process steps to be optimized separately. It is according to the invention
  • an aldehyde of the formula II is reacted with formaldehyde in the presence of base.
  • This implementation is known per se to the person skilled in the art and is advantageously carried out in several stages, as described for example in DE-196 53 093 and EP-A 860419.
  • the aldehyde of formula II is preferably used in the form of an aqueous solution.
  • it is used directly in the form in which it is produced using customary large-scale processes.
  • Formaldehyde is preferably used in the form of an aqueous solution which contains about 1 to 55% by weight, preferably 5 to 35% by weight, particularly preferably 10 to 32% by weight, of formaldehyde.
  • the molar ratio between aldehyde of the formula II and formaldehyde can be, for example, 1: 2 to 1:10, preferably 1: 2 to 1: 5, particularly preferably 1: 2 to 1: 3.5.
  • Suitable bases are, for example, those which act as basic catalysts for the
  • Aldol condensation are known. Alkali and earth alkali metal hydroxides, alkali and alkaline earth metal bicarbonates, alkali and alkaline earth metal carbonates and tertiary amines. Sodium hydroxide, calcium hydroxide, sodium bicarbonate, sodium carbonate and trialkylamines with 1 to 6 carbon atoms per alkyl group are preferred, particularly preferably sodium hydroxide, calcium hydroxide and trialkylamines with 1 to 4 carbon atoms per alkyl group and particularly preferably calcium hydroxide and trialkylamines with 1 to 2 carbon atoms per alkyl group, with above all Trimethylamine and triethylamine may be mentioned.
  • a base but also mixtures of two or more bases, can be used.
  • the bases can be used, for example, in an amount of 0.001 to 0.5 mol per mol of aldehyde of the formula II. 0.01 to 0.4 mol of base per mol of aldehyde are preferred, particularly preferably 0.05 to 0.2 molar equivalents.
  • the concentration of the organic components in the reaction mixture can be, for example, 5 to 50% by weight, preferably 10 to 40% by weight.
  • the reaction can be carried out, for example, at a temperature of 0 to 130 ° C., preferably 10 to 100 ° C., particularly preferably 10 to 80 ° C.
  • the first step of the process according to the invention can be carried out under increased pressure.
  • a particularly high space-time yield and a high yield of 2,2-dimethylolalkanal of the formula III can be achieved by special control of the reaction temperature.
  • the first step of the method according to the invention is therefore preferably started at a relatively low temperature, for example at 0 to 60 ° C., and the temperature is then raised continuously or in stages, the final temperature not to exceed 130 ° C.
  • the desired end temperature temperature can be reached, for example, after a time of 10 minutes to 3 hours.
  • the pH of the reaction mixture is adjusted to between 8 and 12.
  • the pH can be adjusted by adding the bases mentioned above. For this it may be necessary to add the base in several subsets in succession.
  • the residence time of the reaction mixture in the reactor can be, for example, 10 minutes to 10 hours.
  • reaction apparatuses known to the person skilled in the art which are suitable for converting liquid reactants are suitable as reaction apparatuses
  • stirred tank reactor the stirred tank cascade, the flow tube and the multi-chamber reactor or the combination of the apparatuses should be mentioned in particular.
  • the first step of the process according to the invention is preferably carried out only up to a degree of conversion of 40 to 80%, preferably 50 to 70% - defined as the molar ratio of reacted aldehyde of the formula II to the aldehyde of the formula II used - and the unreacted aldehyde of the formula II together separated from the reaction product with optionally formed as a by-product in the 2-position substituted acrylaldehyde.
  • the separation can be carried out by phase separation, the organic phase, which essentially contains aldehyde of the formula II, 2-methylolalkanal and the resulting 2-position substituted acrylaldehyde, is separated from the aqueous phase, which is predominantly 2,2-dimethylolalkanal Contains formula III and formaldehyde.
  • the separated organic phase is returned. If appropriate, all or part of the organic phase can be subjected to distillation before the recycling, the distillate formed being recycled.
  • the separation can also be carried out by distillation. This distillation is preferably carried out as a rectification, for example batchwise or continuously.
  • the rectification can be carried out, for example, at a pressure of 0.01 to 50 bar, preferably between 0.1 and 10 bar.
  • the organic phase to be recycled or its distillate can be returned directly to the first reaction stage or can be pretreated in a separate reaction stage first, as is known from DE-A 196 53 093 and EP-A 860 419.
  • Formula III with respect to the aldehyde of formula II used is generally> 90%, preferably> 95%.
  • 2,2-Dimethylolalkanal is present in the aqueous phase of the resulting reaction mixture.
  • the content of 2,2-dimethylolalkanal of the formula III in the aqueous phase is preferably 5-60% by weight, preferably 15-40% by weight.
  • the 2,2-dimethylolalkanal of the formula III can be isolated, for example by distillation.
  • the aqueous phase is preferably separated off from the first reaction step and fed to the second step of the process according to the invention without isolating the 2,2-dimethylolalkanal of the formula III.
  • the 2,2-dimethylolalkanal of the formula III obtained from the first step is reacted with calcium hydroxide and formaldehyde to give the corresponding trimethylolalkane of the formula I.
  • the 2,2-dimethylolalkanal of the formula III is preferably used in aqueous solution.
  • the molar ratio of 2,2-dimethylolalkanal of the formula III to formaldehyde can be, for example, 1: 1 to 1: 5, preferably 1: 1 to 1: 3, particularly preferably 1: 1 to 1: 1.5.
  • the formaldehyde is preferably used in the form of an aqueous solution which contains, for example, 1 to 55% by weight, preferably 5 to 35% by weight, particularly preferably 10 to 32% by weight of formaldehyde.
  • the aqueous solution of 2,2-dimethylolalkanal of the formula III obtained from the first reaction step contains formaldehyde which has not completely reacted and / or has not yet been completely separated. If such solutions are used in the second reaction step, less formaldehyde has to be added in order to set the molar ratios given above.
  • the procedure can be such that an excess of formaldehyde is used in the first reaction step; the excess is preferably chosen such that no further formaldehyde has to be added in the second reaction step.
  • Process represents, since the selectivity of the first reaction step increases with the excess formaldehyde.
  • the amount of calcium hydroxide added can be, for example, 0.4 to 1 molar equivalents, preferably 0.5 to 0.7, particularly preferably 0.5 to 0.6 molar equivalents, based on the 2,2-dimethylolalkanal of the formula III.
  • the second step of the process according to the invention can be carried out, for example, at temperatures from 10 to 130 ° C., preferably 10 to 80 ° C., particularly preferably 10 to 70 ° C. If the selected reaction temperature exceeds the boiling point of the components of the reaction mixture, the second step of the process according to the invention can be carried out under increased pressure.
  • This step can be carried out continuously, semi-batchwise or batchwise in known reaction apparatuses, for example stirred tank reactors, stirred tank cascades or multi-chamber reactors or a combination of these apparatuses.
  • the residence time in the reactor can be, for example, 5 minutes to 10 hours, preferably 10 minutes to 5 hours.
  • 2-methylolalkanal is present as a secondary component in the aqueous solution of the 2,2-dimethylolalkanal of the formula III from the first reaction step of the process according to the invention, this does not impair the second step.
  • 2-Methylolalkanal is also converted into the desired trimethylolalkane under the conditions for the second reaction step. If 2-methylolalkanal is present in the 2,2-dimethylolalkanal solution, the 2,2-dimethylolalkanal of formula III present is the existing 2 in the above statements of molar ratios of 2,2-dimethylolalkanal to formaldehyde and to calcium hydroxide -Methylolalkanal add.
  • an aqueous suspension which essentially consists of the calcium formate formed and the unreacted one
  • Formaldehyde trimethylolalkane of formula I contains.
  • reaction products trimethylolalkane of the formula I and calcium formate can be isolated as pure substances in a manner known per se.
  • the process according to the invention has proven particularly advantageous for the preparation of trimethylolpropane starting from n-butyraldehyde and formaldehyde.
  • 2,2-dimethylolalkanal is known.
  • n-butyraldehyde and formaldehyde can be converted into 2,2-dimethylolbutanal in the presence of catalytic amounts of a tertiary amine. The so obtained
  • 2,2-Dimethylolbutanal can be used in the second step of the process according to the invention.
  • 2,2-dimethylolalkanal solutions which have been prepared by other known processes in the second step of the process according to the invention.
  • the following examples show that, starting from aqueous 2,2-dimethylolbutanal solutions, trimethylolpropane is obtained in yields of greater than 93% in the second step of the process according to the invention.

Landscapes

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

Abstract

La présente invention concerne un procédé en deux étapes servant à préparer des triméthylolalcanes de formule générale (I), (HOCH2)3-C-R, dans laquelle R est méthylol, alkyle C1-C12, aryle C6-C10 ou aralkyle C7-C22, avec la formation concourante de formiate de calcium à partir d'un aldhéhyde de formule (II), RCH2CHO, dans laquelle R correspond aux éléments mentionnés ci-dessus. Dans une première étape, un aldhéhyde de formule (II) et un formaldéhyde en présence d'une base, sont convertis en un 2,2-diméthylolalcanal de formule (III) dans laquelle R correspond aux éléments mentionnés ci-dessus. Dans une seconde étape, on fait réagir le composé de formule (III) avec du formaldéhyde en présence d'hydroxyde de calcium. Ce procédé permet d'obtenir des triméthylolalcanes de formule générale (I) d'une grande pureté, avec un rendement élevé.
EP01907401A 2000-01-14 2001-01-03 Procede de preparation de trimethylolalcanes Withdrawn EP1250301A1 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE10001257 2000-01-14
DE10001257A DE10001257A1 (de) 2000-01-14 2000-01-14 Verfahren zur Herstellung von Trimethylolalkanen
PCT/EP2001/000016 WO2001051438A1 (fr) 2000-01-14 2001-01-03 Procede de preparation de trimethylolalcanes

Publications (1)

Publication Number Publication Date
EP1250301A1 true EP1250301A1 (fr) 2002-10-23

Family

ID=7627456

Family Applications (1)

Application Number Title Priority Date Filing Date
EP01907401A Withdrawn EP1250301A1 (fr) 2000-01-14 2001-01-03 Procede de preparation de trimethylolalcanes

Country Status (9)

Country Link
US (1) US20030009062A1 (fr)
EP (1) EP1250301A1 (fr)
JP (1) JP2003525876A (fr)
KR (1) KR20020063004A (fr)
CN (1) CN1395550A (fr)
AU (1) AU2001235391A1 (fr)
CA (1) CA2396947A1 (fr)
DE (1) DE10001257A1 (fr)
WO (1) WO2001051438A1 (fr)

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Publication number Priority date Publication date Assignee Title
SE0301102D0 (sv) 2003-04-14 2003-04-14 Tetra Laval Holdings & Finance Method in connection with the production of a apckaging laminate thus produced and a packaging container manufactures from the packaging laminate
DE10317543A1 (de) 2003-04-16 2004-11-04 Basf Ag Verfahren zur Hydrierung von Methylolalkanalen
DE102006009838A1 (de) * 2006-03-01 2007-09-06 Basf Ag Verfahren zur Hydrierung von Methylolalkanalen
US7388116B2 (en) * 2006-06-06 2008-06-17 Basf Aktiengesellschaft Hydrogenation of methylolalkanals
JP2011528745A (ja) 2008-07-23 2011-11-24 ビーエーエスエフ ソシエタス・ヨーロピア ポリマーを製造するための２−イソプロピル−２−アルキル−１，３−プロパンジオールの使用
JP2013526506A (ja) 2010-05-12 2013-06-24 ビーエーエスエフ ソシエタス・ヨーロピア ネオペンチルグリコールの製造方法
US8853465B2 (en) 2010-05-12 2014-10-07 Basf Se Process for preparing neopentyl glycol
CN102304022A (zh) * 2011-07-05 2012-01-04 上海华谊（集团）公司 一种缩合加氢法制备三羟甲基丙烷反应过程中副产物2-乙基丙烯醛的回收利用方法
CN102887819B (zh) * 2011-07-23 2014-08-06 万华化学集团股份有限公司 一种制备2,2-二羟甲基丁醛的方法
WO2013026758A1 (fr) 2011-08-23 2013-02-28 Basf Se Procédé de production de néopentylglycol
US9056824B2 (en) 2013-01-31 2015-06-16 Eastman Chemical Company Preparation of hydroxy aldehydes
US8710278B1 (en) 2013-01-31 2014-04-29 Eastman Chemical Company Process for producing polyols
DE102013021512A1 (de) 2013-12-18 2015-06-18 Oxea Gmbh Verfahren zur Herstellung von 3-Hydroxyalkanalen
DE102013021509B4 (de) 2013-12-18 2020-10-01 Oxea Gmbh Verfahren zur Herstellung von 3-Hydroxyalkanalen
DE102015000810B4 (de) 2015-01-23 2021-05-27 Oq Chemicals Gmbh Verfahren zur Herstellung von 3-Hydroxyalkanalen
DE102015000809A1 (de) 2015-01-23 2016-07-28 Oxea Gmbh Verfahren zur Herstellung von 3-Hydroxyalkanalen
KR102359896B1 (ko) * 2017-10-12 2022-02-07 주식회사 엘지화학 디메틸올부탄알의 제조방법 및 이를 이용한 트리메틸올프로판의 제조방법
CN110878005B (zh) * 2019-12-09 2022-05-03 赤峰瑞阳化工有限公司 一种三羟甲基丙烷和双三羟甲基丙烷连续缩合工艺

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Also Published As

Publication number Publication date
WO2001051438A1 (fr) 2001-07-19
DE10001257A1 (de) 2001-07-19
CA2396947A1 (fr) 2001-07-19
KR20020063004A (ko) 2002-07-31
AU2001235391A1 (en) 2001-07-24
US20030009062A1 (en) 2003-01-09
JP2003525876A (ja) 2003-09-02
CN1395550A (zh) 2003-02-05

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