WO2001066503A2 - Verfahren zur herstellung geradkettiger aliphatischer carbonsäuren aus aldehyden - Google Patents
Verfahren zur herstellung geradkettiger aliphatischer carbonsäuren aus aldehyden Download PDFInfo
- Publication number
- WO2001066503A2 WO2001066503A2 PCT/EP2001/001940 EP0101940W WO0166503A2 WO 2001066503 A2 WO2001066503 A2 WO 2001066503A2 EP 0101940 W EP0101940 W EP 0101940W WO 0166503 A2 WO0166503 A2 WO 0166503A2
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- aldehydes
- oxidation
- straight
- aldehyde
- chain
- Prior art date
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/16—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation
- C07C51/21—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen
- C07C51/23—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of oxygen-containing groups to carboxyl groups
- C07C51/235—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of oxygen-containing groups to carboxyl groups of —CHO groups or primary alcohol groups
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/582—Recycling of unreacted starting or intermediate materials
Definitions
- the present invention relates to a new, non-catalytic process for the production of straight-chain aliphatic carboxylic acids from aldehydes by oxidation with gas mixtures containing oxygen or oxygen.
- Aldehydes are widely used as starting materials for the production of carboxylic acids.
- the preferred position for this area of application owes aldehydes to their high availability following a number of processes, including those used in industry.
- the carbonyl group of the aldehydes can easily be converted into the carboxyl group characteristic of carboxylic acids.
- the conversion of aldehydes to carboxylic acids takes place predominantly in the presence of catalysts.
- processes are also known in which the use of catalysts is dispensed with. In order to avoid side reactions, both the catalytic and the non-catalytic processes are carried out at the lowest possible temperatures, in general a reaction temperature of 100 ° C. is not exceeded.
- the main catalysts used are salts of transition metals, in particular salts of cobalt and manganese as well as chromium, iron, copper, nickel, silver and vanadium.
- the carboxylic acid formation from aldehydes is often associated with side and degradation reactions, even if the optimum temperature conditions are maintained. This applies equally to reactions in the presence as well as in the absence of catalysts. In such cases, the selectivity of the reaction can be considerably improved by adding alkali metal salts of weak acids to the reactants.
- a disadvantage of this process variant, however, is that the salts have an inhibiting effect, so that long reaction times are required for a complete conversion of the starting materials.
- the corresponding aldehydes are oxidized with oxygen in pure form or with air to produce aliphatic monocarboxylic acids having 6 to 9 carbon atoms.
- a combination of manganese and copper compounds which are soluble in the acid acts as a catalyst, the molar ratio of manganese to copper being in the range from 5: 1 to 0.5: 1.
- the starting materials are reacted in the liquid phase at temperatures of about 50 to 80 ° C. and pressures in the range of about 1.4 to 10.3 bar.
- the main difficulty of this process in the process description is the presence of copper and also manganese compounds in the reaction product, i.e. in the carboxylic acid. Elaborate cleaning measures are required to remove the metals, for example their precipitation with aqueous oxalic acid.
- Another catalytic process for reacting aldehydes with oxygen to form carboxylic acids is the subject of the disclosed international application WO97 / 14668.
- Substituted or unsubstituted alkylamines, alkylamine N-oxides, aromatic amines, aromatic N-oxides, heterocyclic amines, heterocyclic amine N-oxides and mixtures thereof use. It is expressly pointed out that the catalytically active nitrogen compounds must have a higher boiling point than the reaction product in order to prevent contamination of the acid by the catalyst.
- branched aliphatic aldehydes are oxidized with oxygen in the presence of lithium or alkaline earth metal compounds which are used in amounts of 0.01 to 10% by weight (based on the entire reaction system) To produce ⁇ -branched aliphatic carboxylic acids.
- Characteristic of the procedure described in French patent application 2 769 624 is the maintenance of low reaction temperatures, namely temperatures between 0 and 25 ° C.
- the process also requires the presence of alkali metal or alkaline earth metal compounds as auxiliaries. It remains open what special effects these compounds have, i.e. whether, as is known, they merely improve the selectivity of the reaction or, at the low temperatures chosen, may also increase the reaction rate.
- aldehyde purification is often carried out using addition and condensation products, which are split after the separation step with the aldehydes regressing.
- addition and condensation compounds of the aldehydes are hydrazones, bisulfite adducts (cf. DE 24 59 152) and acetals.
- n-alkanals can be prepared from n / iso-aldehyde mixtures obtained by hydroformylation by treating the aldehyde mixture with non-oxidizing acids.
- the resulting 1,3,5-trioxanes of the straight-chain aldehydes are separated off by fractional crystallization (cf. DE 22 18 305).
- the known processes for the production of carboxylic acids from aldehydes do not meet the technical and economic requirements placed on modern, industrially used processes not only because of the recommendation to preferably use alkanals of the same molecular size and structure.
- the use of catalysts is also associated with complex purification steps to which the reaction product has to be subjected in order to obtain carboxylic acids which can be processed without any problems.
- Non-catalytic processes are often unsatisfactory in terms of turnover and selectivity for the desired product.
- This object is achieved by a process for the preparation of straight-chain aliphatic carboxylic acids having 4 to 11 carbon atoms by oxidation of the corresponding straight-chain aldehydes with gas mixtures containing oxygen or oxygen at 20 to 100 ° C. It is characterized in that the oxidation of the straight-chain aldehydes takes place in the presence of 1 to 30 mol% of branched aldehydes per mol of straight-chain aldehydes.
- the oxidation of n-aldehydes to the corresponding carboxylic acids with pure oxygen or oxygen as a component of gas mixtures can be carried out very selectively and with high conversion and without the use of catalysts.
- the branched aldehydes added to the oxidation mixture according to the invention are preferably saturated and contain 3 to 15, in particular 4 up to 11 carbon atoms in the molecule.
- the use of unsaturated branched aldehydes is not excluded, but it will be limited to exceptional cases. It should be taken into account here that unsaturated compounds tend to form oxygen-containing degradation products in the oxidizing environment rather than saturated compounds. Such side reactions are undesirable because they can lead to contamination of the n-carboxylic acids.
- branched aldehydes is understood to mean, in accordance with the applicable nomenclature rules, alkanals which, in addition to a main chain consisting of adjacent carbon atoms, also have side chains containing one or more carbon atoms.
- the position of these side chains in the molecule, their number and their length is arbitrary. However, because of their easy accessibility, preference is given to using aldehydes whose side chain is located on the ⁇ - or ⁇ -carbon atom (i.e. in the 2- or 3-position), based on the carbonyl group.
- the branched aldehyde usually contains only one side chain. If there are several side chains in the molecule, they can contain the same or different number of carbon atoms.
- methyl and ethyl radicals are preferred as side chains.
- branched aldehydes are isobutyraldehyde, 2-methylbutanal, 3-methylbutanal (iso-valeraldehyde), 2-methylpentanal, 2-methylhexanal, 2-ethylhexanal, 2-methyloctanal, 3,5,5-trimethylhexanal.
- the molecular size of straight-chain and branched aldehyde need not be the same. It is also not necessary to use branched aldehydes. uniform structure and / or molecular size. Rather, mixtures of two or more different branched aldehydes can also be used. It is therefore possible not only to select those branched aldehydes for carrying out the oxidation reaction which, in the form of the branched acids formed from them, can easily be separated from the target product, but also to take into account economic requirements, for example availability and value for money.
- Branched aldehyde is normally added to the reaction mixture in such an amount that the desired ratio of straight-chain / branched aldehyde is obtained. Conversely, if there is an excess of branched aldehyde in the reaction mixture, either an appropriate amount of n-aldehyde can be added or part of the branched aldehyde can be removed. Of course, special cases are also conceivable in which the aldehyde mixture required for the oxidation stage is already present from the manufacturing process.
- the process of the invention is carried out in the temperature range from 20 to 100 ° C. Preferably one works between 20 and 80 ° C, in particular between 40 and 80 ° C.
- the temperature control, constant or variable Temperature can be adapted to the individual requirements of the starting material and the reaction conditions.
- the reaction of the reactants is preferably carried out at atmospheric pressure. However, the application of increased pressure is not excluded. Usually one works in a range from atmospheric pressure to 1.0 MPa, preferably at atmospheric pressure to 0.8 MPa.
- the reaction time required for converting aldehydes to carboxylic acids by the process according to the invention depends, inter alia, on the reaction temperature, the type of starting materials and the quantitative ratio of the reactants to one another. It is normally 30 minutes to 20 hours, in particular 3 to 8 hours.
- the focus of the new process is the oxidation of unbranched C - to Cn aldehydes.
- the origin of the aldehydes is not limited to specific manufacturing processes. Because of their easy accessibility, aldehydes obtained by oxosynthesis, ie by reaction of C 3 - to C-io-olefins with carbon monoxide and hydrogen, are preferred. In this context, it is not critical which specific embodiment of the oxo synthesis was used to obtain the aldehydes, ie whether the reaction was catalyzed by cobalt or rhodium, for example, whether the metals were used alone or together with complexing agents and the catalyst was homogeneously dissolved in the reaction mixture or formed its own, heterogeneous phase.
- the oxidizing agent used is molecular oxygen or gas mixtures which contain molecular oxygen.
- Other constituents of such gas mixtures are inert gases, for example nitrogen, noble gases and carbon dioxide.
- the proportion of the inert components of the oxygen-containing gas mixture is up to 90% by volume, in particular especially 30 to 80 vol%.
- the preferred oxidizing agents are oxygen or air.
- the aldehydes can be used as such or dissolved in a solvent which is inert under the reaction conditions.
- suitable solvents are ketones such as acetone, esters, e.g. Ethyl acetate, hydrocarbons e.g. Toluene and nitro hydrocarbons such as nitrobenzene.
- the concentration of the aldehyde is limited by its solubility in the solvent.
- the process according to the invention can be carried out batchwise or continuously. A return of unreacted reactants is possible in both cases.
- n-aldehyde and branched aldehyde are placed in a suitable reactor, e.g. a tubular reactor provided with an inflow base, which may also contain packing elements, and conducts the oxygen or the oxygen-containing gas mixture from below through the aldehyde.
- a suitable reactor e.g. a tubular reactor provided with an inflow base, which may also contain packing elements, and conducts the oxygen or the oxygen-containing gas mixture from below through the aldehyde.
- a trickle tower containing packing is used as the reactor.
- the aldehyde is trickled down over the filling and simultaneously introduced into the tower in cocurrent or countercurrent, oxygen or an oxygen-containing gas mixture.
- the desired reaction product ie the straight-chain aliphatic carboxylic acid
- the straight-chain acid is isolated from the reaction mixture by conventional methods. Distillation at normal or reduced pressure and carrier vapor distillation, for example in the usual embodiment of steam distillation. Fractional crystallization also makes it possible to separate the main product from the compulsory accompanying substances.
- the following examples describe the preparation of n-pentanoic acid, n-heptanoic acid and n-nonanoic acid by the process according to the invention.
- the corresponding starting aldehydes are reacted in the presence of branched aldehydes as reaction auxiliaries.
- the examples are compared with the results of comparative experiments in which the n-aldehyde alone, ie in the absence of branched aldehyde, was oxidized.
- the respective test results are reproduced by specifying the following parameters:
- the liquid phase oxidation of n-pentanal to n-pentanoic acid was carried out in a bubble column reactor made of glass with an inner diameter of 38 mm and 150 cm in length without addition of catalyst. Depending on the reaction behavior, the jacket side was cooled or heated by a water circuit connected to a heat exchanger, and the internal temperature was kept constant in this way. Oxygen was supplied from below through a glass filter plate with a maximum pore size of 16-40 ⁇ m connected to the bubble column.
- n-pentanal contained 20.04% by weight of 3-methylbutanal (corresponding to a molar ratio of 100 to 25.26).
- the liquid phase oxidation of n-heptanal to n-heptanoic acid was carried out in a bubble column reactor made of glass with an inner diameter of 38 mm and 150 cm in length without addition of catalyst. Depending on the reaction behavior, the jacket side was cooled or heated by a water circuit connected to a heat exchanger, and the internal temperature was kept constant in this way. Oxygen was supplied from below through a glass filter plate with a maximum pore size of 16-40 ⁇ m connected to the bubble column.
- the liquid phase oxidation of n-nonanal to n-nonanoic acid was carried out in a bubble column reactor made of glass with an inner diameter of 38 mm and 150 cm in length without addition of catalyst. Depending on the reaction behavior, the jacket side was cooled or heated by a water circuit connected to a heat exchanger, and the internal temperature was kept constant in this way. The oxygen supply was carried out from below through a glass filter plate connected to the bubble column with a maximum pore size of 16-40 ⁇ m.
Abstract
Description
Claims
Priority Applications (6)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP01919320A EP1263706B1 (de) | 2000-03-04 | 2001-02-21 | Verfahren zur herstellung geradkettiger aliphatischer carbonsäuren aus aldehyden |
AT01919320T ATE309188T1 (de) | 2000-03-04 | 2001-02-21 | Verfahren zur herstellung geradkettiger aliphatischer carbonsäuren aus aldehyden |
AU2001246462A AU2001246462A1 (en) | 2000-03-04 | 2001-02-21 | Method for the synthesis of straight-chain aliphatic carboxylic acids from aldehydes |
DE50107991T DE50107991D1 (de) | 2000-03-04 | 2001-02-21 | Verfahren zur herstellung geradkettiger aliphatischer carbonsäuren aus aldehyden |
JP2001565324A JP4755379B2 (ja) | 2000-03-04 | 2001-02-21 | アルデヒドから直鎖状脂肪族カルボン酸を製造する方法 |
US10/204,495 US6680395B2 (en) | 2000-03-04 | 2001-02-21 | Method for the synthesis of straight-chain aliphatic carboxylic acids from aldehydes |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE10010770.2 | 2000-03-04 | ||
DE10010770A DE10010770C5 (de) | 2000-03-04 | 2000-03-04 | Nichtkatalytisches Verfahren zur Herstellung geradkettiger aliphatischer Carbonsäuren aus Aldehyden |
Publications (2)
Publication Number | Publication Date |
---|---|
WO2001066503A2 true WO2001066503A2 (de) | 2001-09-13 |
WO2001066503A3 WO2001066503A3 (de) | 2002-01-31 |
Family
ID=7633626
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/EP2001/001940 WO2001066503A2 (de) | 2000-03-04 | 2001-02-21 | Verfahren zur herstellung geradkettiger aliphatischer carbonsäuren aus aldehyden |
Country Status (10)
Country | Link |
---|---|
US (1) | US6680395B2 (de) |
EP (1) | EP1263706B1 (de) |
JP (1) | JP4755379B2 (de) |
AT (1) | ATE309188T1 (de) |
AU (1) | AU2001246462A1 (de) |
DE (2) | DE10010770C5 (de) |
ES (1) | ES2252207T3 (de) |
TW (1) | TWI235149B (de) |
WO (1) | WO2001066503A2 (de) |
ZA (1) | ZA200206791B (de) |
Families Citing this family (12)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
KR100682232B1 (ko) * | 2003-06-05 | 2007-02-12 | 주식회사 엘지화학 | 유기산 제조방법 |
PL1773767T3 (pl) | 2004-07-07 | 2016-07-29 | Biocon Ltd | Synteza azowo związanych związków immunoregulacyjnych |
DE102009014626A1 (de) * | 2009-03-24 | 2010-10-07 | Oxea Deutschland Gmbh | Verfahren zur Herstellung aliphatischer Carbonsäuren aus Aldehyden durch Mikroreaktionstechnik |
FR2983478B1 (fr) | 2011-12-01 | 2013-11-15 | Arkema France | Procede de preparation d'aminoacide comprenant une etape d'hydroformylation d'un nitrile gras insature |
FR2983477B1 (fr) | 2011-12-01 | 2013-12-27 | Arkema France | Procede de coupure de chaines grasses insaturees |
DE102013020320B4 (de) | 2013-12-05 | 2019-04-04 | Oxea Gmbh | Verfahren zur Herstellung von 2-Methylbuttersäure mit einem vermindertem Gehalt an 3-Methylbuttersäure aus den bei der Herstellung von Pentansäuren anfallenden Nebenströmen |
DE102013020322B4 (de) | 2013-12-05 | 2019-04-18 | Oxea Gmbh | Verfahren zur Gewinnung von 2-Methylbutanal aus den bei der Herstellung von Gemischen isomerer a,ß-ungesättigter Decenale anfallenden Nebenströmen |
EP3094615A4 (de) | 2014-01-13 | 2017-11-08 | P2 Science, Inc. | Säuren aus terpen und ester sowie verfahren zur herstellung und verwendung davon |
US10071944B2 (en) | 2014-06-20 | 2018-09-11 | P2 Science, Inc. | Film ozonolysis in a tubular or multitubular reactor |
JP7028457B2 (ja) | 2016-06-21 | 2022-03-02 | ピー2・サイエンス・インコーポレイテッド | 過酸化物混合物の連続クエンチのためのフロースルー反応器およびそれを含む方法 |
US10696605B2 (en) | 2016-09-16 | 2020-06-30 | P2 Science, Inc. | Uses of vanadium to oxidize aldehydes and ozonides |
JP2022505298A (ja) | 2018-10-19 | 2022-01-14 | ピー2・サイエンス・インコーポレイテッド | オゾニドの不均化クエンチの新規方法 |
Citations (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE1083800B (de) * | 1958-12-22 | 1960-06-23 | Ruhrchemie Ag | Verfahren zur Herstellung von Gemischen isomerer verzweigtkettiger Nonansaeure |
DE1154454B (de) * | 1959-12-09 | 1963-09-19 | Ruhrchemie Ag | Verfahren zur Herstellung von Gemischen isomerer verzweigter aliphatischer oder cycloaliphatischer Carbonsaeuren |
Family Cites Families (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS4931966B1 (de) * | 1970-03-25 | 1974-08-27 | ||
JPS4931967B1 (de) * | 1970-03-25 | 1974-08-27 | ||
DE3029700A1 (de) * | 1979-08-09 | 1981-02-26 | Celanese Corp | Katalytisches verfahren zur herstellung gesaettigter aliphatischer monocarbonsaeuren mit 6 bis 9 c-atomen |
-
2000
- 2000-03-04 DE DE10010770A patent/DE10010770C5/de not_active Expired - Fee Related
-
2001
- 2001-02-21 AT AT01919320T patent/ATE309188T1/de not_active IP Right Cessation
- 2001-02-21 EP EP01919320A patent/EP1263706B1/de not_active Revoked
- 2001-02-21 WO PCT/EP2001/001940 patent/WO2001066503A2/de active IP Right Grant
- 2001-02-21 AU AU2001246462A patent/AU2001246462A1/en not_active Abandoned
- 2001-02-21 JP JP2001565324A patent/JP4755379B2/ja not_active Expired - Fee Related
- 2001-02-21 ES ES01919320T patent/ES2252207T3/es not_active Expired - Lifetime
- 2001-02-21 US US10/204,495 patent/US6680395B2/en not_active Expired - Fee Related
- 2001-02-21 DE DE50107991T patent/DE50107991D1/de not_active Revoked
- 2001-03-01 TW TW090104628A patent/TWI235149B/zh not_active IP Right Cessation
-
2002
- 2002-08-23 ZA ZA200206791A patent/ZA200206791B/xx unknown
Patent Citations (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE1083800B (de) * | 1958-12-22 | 1960-06-23 | Ruhrchemie Ag | Verfahren zur Herstellung von Gemischen isomerer verzweigtkettiger Nonansaeure |
DE1154454B (de) * | 1959-12-09 | 1963-09-19 | Ruhrchemie Ag | Verfahren zur Herstellung von Gemischen isomerer verzweigter aliphatischer oder cycloaliphatischer Carbonsaeuren |
Also Published As
Publication number | Publication date |
---|---|
TWI235149B (en) | 2005-07-01 |
EP1263706A2 (de) | 2002-12-11 |
AU2001246462A1 (en) | 2001-09-17 |
DE50107991D1 (de) | 2005-12-15 |
DE10010770C5 (de) | 2007-02-22 |
ATE309188T1 (de) | 2005-11-15 |
ES2252207T3 (es) | 2006-05-16 |
DE10010770C1 (de) | 2001-09-13 |
JP2003525919A (ja) | 2003-09-02 |
US6680395B2 (en) | 2004-01-20 |
WO2001066503A3 (de) | 2002-01-31 |
ZA200206791B (en) | 2004-01-28 |
US20030100781A1 (en) | 2003-05-29 |
JP4755379B2 (ja) | 2011-08-24 |
EP1263706B1 (de) | 2005-11-09 |
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