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EP1098867A1 - Procede de production d'acide acrylique - Google Patents

Procede de production d'acide acrylique

Info

Publication number
EP1098867A1
EP1098867A1 EP99939391A EP99939391A EP1098867A1 EP 1098867 A1 EP1098867 A1 EP 1098867A1 EP 99939391 A EP99939391 A EP 99939391A EP 99939391 A EP99939391 A EP 99939391A EP 1098867 A1 EP1098867 A1 EP 1098867A1
Authority
EP
European Patent Office
Prior art keywords
stage
acrylic acid
solution
condensation
crystallization
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Withdrawn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
EP99939391A
Other languages
German (de)
English (en)
Inventor
Bernd Eck
Jörg Heilek
Volker Schliephake
Theo Proll
Klaus BRÖLLOS
Otto Machhammer
Joachim Thiel
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
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 BASF SE filed Critical BASF SE
Publication of EP1098867A1 publication Critical patent/EP1098867A1/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
    • C07C51/42—Separation; Purification; Stabilisation; Use of additives
    • C07C51/43—Separation; Purification; Stabilisation; Use of additives by change of the physical state, e.g. crystallisation

Definitions

  • the present invention relates to a process for the production of acrylic acid.
  • Acrylic acid is an important basic chemical. Because of its highly reactive double bond and the acid function, it is particularly suitable as a monomer for the preparation of polymers. Of the amount of acrylic acid monomers produced, the greater part before the polymerization - to z. B. adhesives, dispersions or paints - esterified. Only the smaller part of the acrylic acid monomers produced is directly - to z. B. "Superabsorbers" - polymerized. While monomers of high purity are generally required in the direct polymerization of acrylic acid, the requirements for the purity of acrylic acid are not so high if it is esterified before the polymerization.
  • 400 ° C can be produced in one or two stages using acrolein (see e.g.
  • oxidic multi-component catalysts z. B. on the basis of oxides of the elements molybdenum, bismuth and iron (in the 1st
  • this amount of solids can be reduced by adding a polar solvent such as dimethyl phthalate in an amount of 0.1 to 25% by weight to the relatively non-polar solvent mixture of diphenyl ether and diphenyl.
  • a polar solvent such as dimethyl phthalate
  • a disadvantage of the processes described above is that an organic solvent is used for the extraction or absorption, which is used in a further process. level as a rectification is separated again at high thermal stress. There is a risk of polymerization of the acrylic acid.
  • JP-A-07 082 210 describes a process for purifying acrylic acid which, in addition to acrylic acid, contains acetic acid, propionic acid, acrolein and furfural. In this process, crystallization is carried out in vacuo after the addition of water, a purity of 99.6% being achieved after removal and washing of the acrylic acid crystals.
  • Japanese Patent 45-32417 discloses a method in which an aqueous acrylic acid solution which additionally contains acetic acid and propionic acid is extracted with heptane or toluene, and then water is removed from the extract by distillation. In the next stage, the remaining extract is cooled to -20 to -80 ° C in order to bring about a crystallization of acrylic acid.
  • the acrylic acid used for crystallization is hereby produced by conventional methods, for example by gas phase oxidation of propene or acrolein, and then a pre-cleaning by conventionally known methods, e.g. B. extraction.
  • the crystallization of acrylic acid is preferably carried out essentially in the absence of water.
  • EP-A-0 616 998 describes a process for the purification of acrylic acid by means of a combination of dynamic and static crystallization, wherein pre-purified acrylic acid, for example acrylic acid pre-purified by distillation, is used as the starting product.
  • EP-A-0 002 612 which relates to a process for the purification of acrylic acid present in aqueous solution by fractional crystallization, discloses the addition of salts to the acrylic acid solution in order to break up the eutectic water-acrylic acid, which is 63% by volume acrylic acid.
  • EP-A-0 675 100 describes a process for the preparation of ⁇ -unsaturated C 3 -C 6 carboxylic acids, e.g. As acrylic acid, by oxidative dehydrogenation of the corresponding saturated C 3 -C 6 carboxylic acid followed by melt crystallization with subsequent fractional distillation or followed by fractional distillation with subsequent melt crystallization.
  • the object of the present invention was to provide a process in which acrylic acid is obtained in high purity without complex process steps.
  • Product mixture which is subjected to condensation can be crystallized directly from the solution formed during the condensation. In particular it was found that no further cleaning step and no addition of auxiliary substances are required for this.
  • the invention thus relates to a process for the preparation of acrylic acid by:
  • step (c) crystallization of the acrylic acid from the solution obtained in step (b) with partial evaporation of the solution in vacuo
  • the condensation in stage (b) is carried out in a column. Further preferred embodiments of the invention result from the following description, the subclaims, the figure and the example.
  • the acrylic acid is crystallized directly and immediately from the solution without further intermediate or purification stages and without the addition of auxiliaries, which is formed during the condensation of the product mixture.
  • This product mixture essentially has the composition of a reaction product resulting from the catalytic gas phase oxidation to the acid.
  • the single figure shows a preferred exemplary embodiment for carrying out the method according to the invention.
  • high and low boilers, medium boilers and low boilers as well as corresponding adjective terms mean compounds / substances which have a higher boiling point than acrylic acid (high boilers) or those which have approximately the same boiling point as acrylic acid (middle boilers) or those with a lower boiling point than acrylic acid (low boilers).
  • a gaseous product mixture is produced which essentially has the composition of a reaction mixture for the catalytic gas phase oxidation of C 3 -alkanes, -alkenes, -alkanols and / or -alkanals and / or precursors thereof to give acrylic acid.
  • the gaseous product mixture is particularly advantageously produced by catalytic gas phase oxidation of propene, propane or acrolein. All precursors of the above-mentioned C compounds can be used as starting compounds, in which the actual C - starting compound only forms intermediately during the gas phase oxidation.
  • Acrylic acid can be made directly from propane.
  • heterogeneous catalysts are oxidic multicomponent catalysts based on the oxides of molybdenum, bismuth and iron in the 1st stage (oxidation of propene to acrolein) and the oxides of molybdenum and vanadium used in the 2nd stage (oxidation of acrolein to acrylic acid). These implementations are carried out, for example, in one or two stages. If propane is used as the starting material, it can be converted to a propene / propane mixture by: catalytic oxide hydrogenation, such as.
  • Suitable propene / propane mixtures are also refinery propene (70% propene and 30% propane) or cracked propene (95% propene and 5% propane).
  • propene / propane mixtures such as those mentioned above can be oxidized to acrolein and acrylic acid using oxygen or air or a mixture of oxygen and nitrogen of any composition.
  • propane acts as a diluent and / or reactant.
  • a suitable process is also described in EP-B-0 608 838, in which propane is reacted directly as a reactant to give acrylic acid.
  • the conversion of propene to acrylic acid is very exothermic.
  • the reaction gas which in addition to the starting materials and products advantageously an inert diluent gas, for. B. cycle gas (see below), atmospheric nitrogen, one or more saturated C 6 -C 6 hydrocarbons, especially methane and / or propane, and / or water vapor, can therefore only absorb a small part of the heat of reaction.
  • the type of reactors used is not limited per se, shell-and-tube heat exchangers that are filled with the oxidation catalyst are mostly used, since the majority of the heat released during the reaction can be dissipated to the cooled tube walls by convection and radiation.
  • the reaction product mixture usually contains, based in each case on the total reaction mixture, 1 to 30% by weight of acrylic acid, 0.05 to 1% by weight of propene and 0.05 to 1% by weight of acrolein, 50 to 98% by weight inert diluent gases, 0.05 to 10% by weight oxygen, 0.05 to 2% by weight acetic acid, 0.01 to 2% by weight propionic acid, 0.05 to 1% by weight formaldehyde, 0.05 up to 2% by weight of aldehydes and 0.01 to 0.5% by weight of maleic anhydride.
  • Inert diluent gases are, in particular, saturated C 1 -C 6 -hydrocarbons, such as 0 to 90% by weight of methane and / or propane, in addition 1 to 30% by weight of water vapor, 0.05 to 15% by weight of carbon oxides and 0 to 90 wt .-% nitrogen, each based on 100 wt .-% diluent.
  • saturated C 1 -C 6 -hydrocarbons such as 0 to 90% by weight of methane and / or propane, in addition 1 to 30% by weight of water vapor, 0.05 to 15% by weight of carbon oxides and 0 to 90 wt .-% nitrogen, each based on 100 wt .-% diluent.
  • step (b) the reaction product obtained in step (a) is subjected to condensation, in particular partial or total condensation, a solution being obtained.
  • the condensation is preferably carried out in a column.
  • a column with separating internals in particular with packings, packing elements and / or trays, preferably bubble trays, sieve trays, valve trays and / or dual-flow trays, is used.
  • the condensable components of the gaseous product mixture from stage (a) are fractionally condensed out by cooling. Since the gas mixture contains a high boiler, medium boiler and low boiler fraction as well as non-condensable components as a result of the impurities and dilution gases, one or more side draws can be provided in the column at the appropriate points.
  • a condensation in a column thus already enables the individual components to be separated.
  • Suitable Columns comprise at least one cooling device, for which all common heat exchangers or heat exchangers in which the heat generated during the condensation is dissipated indirectly (externally) are suitable. Tube bundle heat exchangers, plate heat exchangers and air coolers are preferred. Suitable cooling media are air in the corresponding air cooler and cooling liquids, in particular water, in other cooling devices. If only one cooling device is provided, this is installed at the top of the column by condensing out the low boiler fraction. Since the acrylic acid-containing gas mixture contains several fractions, it is advisable to install several cooling devices in different sections of the column, e.g. B.
  • the fraction with the acrylic acid is drawn off in the central part of the column via one or more side draws.
  • the pressure in the column depends on the amount of non-condensable components and is preferably 0.5-5 bar absolute pressure, in particular 0.8-3 bar absolute pressure.
  • the hot gas mixture is cooled directly or indirectly before the condensation.
  • direct cooling it is preferable that the gas mixture is cooled using the high boiler fraction condensed from the gas mixture. In the other case, an adjuvant is entered in the process, but must be worked up again.
  • this pre-cooling can be integrated in the bottom region of the column (with or without column internals) or separately from the column in a separate apparatus, for. B. a gas cooler, a quench or a flash pot.
  • a gas cooler a quench or a flash pot.
  • the hot gas mixture is introduced in the bottom area and cooled. This can be done via indirect cooling, e.g. B. heat exchanger, or direct cooling with in the next section of the column condensed high boiler fraction as
  • Cooling medium take place.
  • the heat of condensation is externally via the first cooling circuit by means of a heat exchanger with z.
  • water is removed as the cooling medium by removing condensed high boiler fraction from the column, cooling by means of the heat exchanger and recycling part of the cooled, condensed high boiler fraction to the column, while the other part, usually less than 1% by weight, based on 100 % By weight of condensate in the side outlet, is discharged.
  • the recirculated, condensed high boiler fraction is conducted in countercurrent to the rising gas.
  • the acrylic acid is removed via the side vent.
  • the medium boiler fraction is enriched from the gas stream which is led upward in countercurrent, the middle boiler fraction being enriched toward the side drain.
  • the low boiler fraction In the area of the second cooling circuit, the low boiler fraction is condensed from the gas stream which is led upward in countercurrent.
  • the heat of condensation is external via the second cooling circuit by means of a
  • Heat exchanger with z. B. water is removed as a cooling medium by withdrawing the condensed low boiler fraction, cooling and recycling part of the cooled, condensed low boiler fraction while the other part is being discharged.
  • the uncondensed components which are preferably nitrogen, carbon monoxide,
  • Carbon dioxide, oxygen, methane, propane and propene are traded by the Head of the column withdrawn.
  • condensation can be carried out in one or more stages using customary methods, the type of condensation being not subject to any particular restriction.
  • the condensation is advantageously carried out using a direct condenser, the condensate already produced being brought into contact with the hot gaseous reaction product.
  • Spray washers, venturi washers, bubble columns or apparatuses with sprinkled surfaces are particularly suitable as apparatuses for the condensation.
  • the mixture obtained by partial or total condensation of the reaction product from stage (a), in particular the condensate of the medium boiler fraction when condensed in a column preferably contains 60 to 99.5% by weight of acrylic acid and 0.1 to 40% by weight of water , in addition 0.1 to 15% by weight of impurities, in particular, based in each case on 100% by weight of condensate, 0.01 to 5% by weight of acrolein, 0.05 to 5% by weight of acetic acid, 0.01 up to 5% by weight of propionic acid, 0.01 to 5% by weight of formaldehyde, 0.01 to 5% by weight of further aldehydes and 0.01 to 5% by weight of maleic acid.
  • a mixture which contains 85 to 98% by weight of acrylic acid, 0.5 to 14% by weight of water and, in addition, 0.5 to 5% by weight of impurities, in particular based on 100% by weight, is particularly preferably obtained in the condensation % Condensate, 0.01 to 3% by weight acrolein, 0.1 to 3% by weight acetic acid, 0.01 to 3% by weight propionic acid, 0.01 to 3% by weight formaldehyde, 0 , 01 to 3 wt .-% further aldehydes and 0.01 to 3 wt .-% maleic acid.
  • step (c) the solution obtained in step (b), which is enriched in acrylic acid, is crystallized.
  • This solution obtained in the condensation stage is thus fed directly to the crystallization.
  • the crystallization can be carried out continuously or batchwise, in one stage or in multiple stages. This is preferably done Single stage crystallization. All crystallization processes in which the crystallizing solution / melt is mixed by stirring or circulating are suitable, both in the case of a continuous and a batchwise procedure. Stirred tank crystallizers and forced circulation crystallizers are preferably used as apparatuses, but guide tube and fluidized bed crystallizers can also be used.
  • the solution is partially evaporated in the crystallization. This results in a boiling temperature of the crystallizing solution, which depends on the pressure in the crystallization.
  • the pressure in the crystallization is brought to the desired value by means of a vacuum generator.
  • the device for vacuum generation is not subject to any restrictions. All systems are suitable which achieve the desired vacuum in one or more stages by mechanical and / or thermal compression.
  • Liquid ring pumps are preferably used, in particular in combination with steam jet pumps, steam jet pumps alone or Roots or rotary vane pumps.
  • the pressures to be set depend on the composition of the crystallizing solution. Expediently they are between 1 and 15 mbar (absolute), preferably between 3 and 8 mbar (absolute).
  • the temperature of the solution during the crystallization is advantageously between -10 ° C. and +14 ° C., in particular between -5 ° C. and +10 ° C.
  • the crystallization is advantageously carried out in such a way that a solids content of between 5 and 60 g of solids per 100 g of suspension is established, contents of between 15 and 45 g of solids per 100 g of suspension being preferred.
  • stage (d) the acrylic acid crystals obtained in stage (c) are removed from the Mother liquor separated. All known methods of solid-liquid separation are suitable for this.
  • the crystals are separated from the mother liquor by filtration and / or centrifugation.
  • the filtering or centrifuging is advantageously preceded by a pre-thickening of the suspension, for example by hydrocyclone (s). All known centrifuges that work discontinuously or continuously are suitable for centrifugation. Shear centrifuges which can be operated in one or more stages are most advantageously used. Screw sieve centrifuges or screw discharge centrifuges (decanters) are also suitable. Filtration is advantageously carried out by means of suction filters, which are operated batchwise or continuously, with or without an agitator, or by means of a belt filter. In general, the filtering can be carried out under pressure or in vacuo.
  • the crystals or the crystal cake are washed and / or sweated in one or more stages.
  • the amount of washing liquid is suitably between 0 and 500 g of washing liquid / 100 g of crystals, preferably between 30 and 200 g of washing liquid / 100 g of crystals.
  • the washing liquid used is not subject to any restrictions.
  • washing with pure product ie with a liquid which contains acrylic acid, the purity of which is higher than that of the crystal cake to be washed, but is at least purer than the mother liquor in the crystallization. Washing with water is also possible. Washing can be carried out in the usual apparatus for this.
  • washing columns in which the mother liquor is separated and washed in one apparatus centrifuges which can be operated in one or more stages, or filter filters or belt filters are used. Washing can be carried out on centrifuges or belt filters in one or more stages.
  • the washing liquid can be passed in countercurrent to the crystal cake. Sweating is a local melting of contaminated areas.
  • the amount of sweat is between 0 and 100 g of melted crystals / 100 g of crystals before sweating, preferably between 5 and 35 g of melted crystals / 100 g of crystals. Sweating on centrifuges or belt filters is particularly preferred. Carrying out a combination of washing and sweating in one apparatus can also be suitable.
  • the acrylic acid crystals after the solid-liquid separation and possibly further washing and / or sweating represent the purified acid from the process.
  • the purity of the crystals obtained is generally 97 to 99.99% by weight of acrylic acid, in particular 98% 5 to 99.9% by weight acrylic acid.
  • the crystals produced by the process according to the invention now contain only very small amounts of impurities, such as acetic acid, maleic acid or aldehydes.
  • the purified acid can be esterified by known methods or further purified by known methods.
  • stage (e) the mother liquor remaining after the crystals have been separated off from stage (d) is at least partially returned directly to the condensation stage (b).
  • the proportion of the returned mother liquor is between 0 and 100% by weight, in particular 80 to 100% by weight, preferably it is 100% by weight.
  • the mother liquor is expediently recycled below the side draw of the column, preferably into the area between the first cooling circuit and the side draw, most preferably into the area just below or a few trays below the side draw of the column.
  • Level ff :
  • stage (f) at least part of the solution evaporated in stage (c) is returned to the condensation stage (b).
  • the proportion of the solution returned to stage (b) is between 0 and 100% by weight, in particular between 50 and 100% by weight, preferably between 80 and 100% by weight, and most preferably about 100% by weight. -%.
  • the evaporated solution is expediently recycled above the side draw of the column, preferably in the area between the side draw and the second cooling circuit, most preferably in the area just above or a few trays above the side draw of the column.
  • the part of the evaporated solution which is not returned to stage (b) is advantageously returned to the crystallization stage (c).
  • there is also the possibility of discharging evaporated solution expediently not more than 80% by weight of the evaporated solution being discharged.
  • stage (b) and optionally stage (c) The return of the vaporized solution to stage (b) and optionally stage (c) is not subject to any restrictions with regard to the phase state (gaseous, partially condensed, fully condensed).
  • the return in the liquid state is preferably carried out after carrying out a partial or total condensation of the evaporated solution.
  • the condensation processes and apparatuses and the generation of the mass and heat exchange surfaces required for the condensation are not subject to any restrictions.
  • the exchange area (s) can be in
  • Spraying liquids such as B. already obtained condensate and / or
  • At least 90% of the evaporated solution is condensed.
  • the entire condensable portion of the vaporized solution is condensed.
  • Non-condensable portions of the evaporated solution are expediently discharged via the vacuum generation device in stage (c).
  • Air is fed to the synthesis reactors 4 and 5 via line 2 and compressor 3.
  • the reactor 4 is fed via line 9 from the compressor 6 recycle gas, which consists essentially of nitrogen, carbon oxides and unreacted starting materials, and propene originating from line 1.
  • the first stage of the two-stage gas phase oxidation takes place in the synthesis reactor 4, namely the oxidation of propene to acrolein.
  • the acrolein is then oxidized to the corresponding acid in the synthesis reactor 5.
  • the capacitor 8 is designed as a column in the figure.
  • the uncondensed part of the product mixture is discharged via line 9, part of which is returned to reactor 4 as circulating gas, as described above, and the other part, preferably 50% of the total flow of line 9, as waste gas from the system via the line 10 is dissipated.
  • the condensed high boiler fraction is removed via line 18, while the condensed low boiler fraction is removed via line 19.
  • the condensed medium boiler fraction which contains most of the acrylic acid, is fed via line 11 (side draw) to the crystallization device 12, in which the crystallization is carried out.
  • the mother liquor from the crystallization is fed together with the crystallizate via line 13 to a suitable apparatus 14 for solid-liquid separation, the crystallizate being discharged via line 15 and the mother liquor being discharged via line 16.
  • At least a part of the mother liquor is fed via line 17 into the condenser 8, preferably below the side draw (line 11), and thus fed back to the condensation.
  • the purified acid is removed via line 15.
  • part of the solution is evaporated under vacuum, which is formed by the vacuum generating device 25, and fed to the condensation device 20 via line 21.
  • the evaporated solution is almost completely in the condensed phase transferred.
  • the condensed phase is partly returned via line 22 to the crystallization device 12, partly via line 23 into the condensation device 8, preferably above the side draw (line 11).
  • the portions of the evaporated solution that are not condensed in the device 20 are fed to the device 25 via line 24 and are discharged from the process via line 26 as waste gas.
  • the present invention enables high yield.
  • the heat released in the crystallization stage is easily removed from the crystallization by partial evaporation of the solution.
  • part of the effort required to separate acrylic acid and (compared to acrylic acid) low boilers is taken over by the partial evaporation of the solution in the crystallization.
  • the process according to the invention also has the advantage over the processes known hitherto that after condensation of the product mixture formed in the gas phase oxidation, an acid of very good quality is obtained directly from the solution formed during the condensation by crystallization.
  • a pure acid can be generated directly, whereby unlike in the above-mentioned documents, Canadian Patent 790 625, JP-A-0 07 082 210-A and EP-A-0 616 998 no pre-cleaning must be done.
  • Another important advantage of the process according to the invention is that the process is carried out relatively cold, ie the main stream of acrylic acid is passed directly from the process as a product via condensation and crystallization. Since, unlike in the prior art, no auxiliary substance is added and therefore no high thermal stress (in particular with high acrylic acid contents) is required to separate this auxiliary substance, polymerization problems and the use of process stabilizers, as occur here in the prior art, are reduced. It also avoids or reduces fouling. It is surprising that acrylic acid solutions obtained by gas phase oxidation and condensation can be crystallized directly and that products of very high purity can be obtained in this way. In particular, it was surprising that this is also possible with aqueous condensates.
  • the invention is illustrated by the following example, which represents a preferred embodiment of the invention.
  • reaction stage (a) The following mixture with a temperature of 270 ° C. was obtained from reaction stage (a) by catalytic gas phase oxidation of propene.
  • the mixture (10867 g / h) was fed to the condensation stage (b).
  • a tray column with 27 bubble-cap trays was used as the condensation apparatus.
  • the temperature in the column bottom was 100 ° C.
  • the heat of condensation was removed via heat exchangers at trays 1 and 27.
  • Phenothiazine was added as a stabilizer above the side draw of the column.
  • a stream of 269 g / h of the following composition was drawn off at base 27:
  • the mixture originating from the bottom 11 was then crystallized in a 10 1 stirred container with a spiral stirrer.
  • the heat of crystallization was removed via partial evaporation.
  • the crystallization temperature of the solution was 6.5 ° C.
  • the pressure was 3 mbar.
  • the suspension produced during the crystallization was separated into crystals and mother liquor on a centrifuge at 2000 rpm (centrifuge diameter 250 mm) and a centrifuging time of 1 min.
  • the crystals (1486 g / h) were then washed with melted crystals (323 g / h) for 1 min at 2000 rpm.
  • the mother liquor was returned together with the washing liquid to the condensation column on tray 10 (3060 g / h).
  • the solution evaporated in the crystallization was returned to tray 15 after condensation in the column (732 g / h).
  • the composition of this stream was:

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

L'invention concerne un procédé de production d'acide acrylique consistant à (a) produire un mélange gazeux ayant sensiblement la composition d'un mélange réactionnel de l'oxydation en phase gazeuse catalytique de C3-alcanes, C3-alcènes, C3-alcanols et/ou C3-alcanals et/ou de leurs précurseurs, permettant d'obtenir de l'acide acrylique. Cette production est caractérisée par (b) la condensation du mélange gazeux; (c) la cristallisation de l'acide acrylique à partir de la solution obtenue en (b) avec évaporation partielle de la solution sous vide; (d) la séparation des cristaux obtenus et de la lessive-mère; (e) renvoi d'au moins une partie de la lessive-mère issue de (d) et (b); et (f) renvoi d'au moins une partie de la solution évaporée issue de (c) et (b).
EP99939391A 1998-07-22 1999-07-21 Procede de production d'acide acrylique Withdrawn EP1098867A1 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE19833049A DE19833049A1 (de) 1998-07-22 1998-07-22 Verfahren zur Herstellung von Acrylsäure
DE19833049 1998-07-22
PCT/EP1999/005204 WO2000005188A1 (fr) 1998-07-22 1999-07-21 Procede de production d'acide acrylique

Publications (1)

Publication Number Publication Date
EP1098867A1 true EP1098867A1 (fr) 2001-05-16

Family

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Family Applications (1)

Application Number Title Priority Date Filing Date
EP99939391A Withdrawn EP1098867A1 (fr) 1998-07-22 1999-07-21 Procede de production d'acide acrylique

Country Status (9)

Country Link
US (1) US6433222B1 (fr)
EP (1) EP1098867A1 (fr)
JP (1) JP4520637B2 (fr)
KR (1) KR20010072021A (fr)
CN (1) CN1311766A (fr)
BR (1) BR9912344A (fr)
DE (1) DE19833049A1 (fr)
ID (1) ID27390A (fr)
WO (1) WO2000005188A1 (fr)

Families Citing this family (26)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE19829477A1 (de) * 1998-07-01 2000-01-05 Basf Ag Verfahren zur Reinigung von Acrylsäure oder Methacrylsäure durch Kristallisation und Destillation
MY122671A (en) 1999-03-06 2006-04-29 Basf Ag Fractional condensation of a product gas mixture containing acrylic acid
DE19926082A1 (de) 1999-06-08 2000-12-14 Basf Ag Verfahren zur Reinigung und Herstellung von Acrylsäure oder Methacrylsäure
BR0109929B1 (pt) * 2000-04-11 2012-08-07 processo para a purificaÇço de uma massa fundida de Ácido acrÍlico bruto.
EP1349826B1 (fr) 2001-01-12 2012-06-27 Evonik Stockhausen GmbH Procede continu pour la production et la purification d'acide (meth)acrylique
US6958414B2 (en) * 2002-12-16 2005-10-25 Basf Aktiengesellschaft Preparation of at least one organic compound by heterogeneously catalyzed partial gas-phase oxidation
JP4415140B2 (ja) * 2003-03-31 2010-02-17 独立行政法人農業・食品産業技術総合研究機構 １−置換−シクロプロペンの効率的処理技術
JP4658104B2 (ja) * 2003-06-05 2011-03-23 株式会社日本触媒 アクリル酸の製造方法
US7183428B2 (en) * 2003-06-05 2007-02-27 Nippon Shokubai Co., Inc. Method for production of acrylic acid
KR100563661B1 (ko) * 2003-12-18 2006-03-23 한국전자통신연구원 가변 고차 베셀 저역 통과 필터
JP2005336142A (ja) * 2004-05-31 2005-12-08 Mitsubishi Chemicals Corp （メタ）アクリル酸の製造装置及び（メタ）アクリル酸の製造方法
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ID27390A (id) 2001-04-05
JP2002521353A (ja) 2002-07-16
DE19833049A1 (de) 2000-01-27
JP4520637B2 (ja) 2010-08-11
KR20010072021A (ko) 2001-07-31
BR9912344A (pt) 2001-04-17
US6433222B1 (en) 2002-08-13
CN1311766A (zh) 2001-09-05

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