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  • C07C51/25—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of unsaturated compounds containing no six-membered aromatic ring
  • C07C51/252—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of unsaturated compounds containing no six-membered aromatic ring of propene, butenes, acrolein or methacrolein
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  • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
  • C07C29/48—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by oxidation reactions with formation of hydroxy groups
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  • C07C409/14—Peroxy compounds the —O—O— group being bound between a carbon atom, not further substituted by oxygen atoms, and hydrogen, i.e. hydroperoxides the carbon atom belonging to a ring other than a six-membered aromatic ring
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  • C07C45/32—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen
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  • C07C45/34—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of CHx-moieties in unsaturated compounds
  • C07C45/35—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of CHx-moieties in unsaturated compounds in propene or isobutene
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  • C07C45/32—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen
  • C07C45/33—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of CHx-moieties
  • C07C45/34—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of CHx-moieties in unsaturated compounds
  • C07C45/36—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of CHx-moieties in unsaturated compounds in compounds containing six-membered aromatic rings
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  • 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
  • C07C51/215—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of saturated hydrocarbyl groups
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  • 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
  • C07C51/255—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of compounds containing six-membered aromatic rings without ring-splitting
  • C07C51/265—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of compounds containing six-membered aromatic rings without ring-splitting having alkyl side chains which are oxidised to carboxyl groups
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  • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
  • B01J2219/00049—Controlling or regulating processes
  • B01J2219/00051—Controlling the temperature
  • B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
  • B01J2219/00087—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements outside the reactor
  • B01J2219/00103—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements outside the reactor in a heat exchanger separate from the reactor
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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  • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
  • B01J2219/00049—Controlling or regulating processes
  • B01J2219/00051—Controlling the temperature
  • B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
  • B01J2219/00105—Controlling the temperature by indirect heating or cooling employing heat exchange fluids part or all of the reactants being heated or cooled outside the reactor while recycling
  • B01J2219/00108—Controlling the temperature by indirect heating or cooling employing heat exchange fluids part or all of the reactants being heated or cooled outside the reactor while recycling involving reactant vapours
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  • B01J2219/00049—Controlling or regulating processes
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  • B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
  • B01J2219/00105—Controlling the temperature by indirect heating or cooling employing heat exchange fluids part or all of the reactants being heated or cooled outside the reactor while recycling
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  • C07C2601/14—The ring being saturated
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  • Y02P20/582—Recycling of unreacted starting or intermediate materials

Definitions

• the present invention relates to a process for the oxidation of a starting material with an oxidizing agent to obtain a product
• a reaction device which has a bottom region at the lower end, a top region at the top end and a reaction zone between the bottom region and the top region,
• saturated compounds to unsaturated compounds such as methylcyclohexane to toluene or propane to propene
• alcohols to aldehydes or ketones such as isopropanol to acetone, s-butanol to methyl ethyl ketone or methanol to formaldehyde
• hydrocarbons to hydroperoxides such as Cu ol to cumene hydroperoxide, tetralin to tetralin hydroperoxide or cyclohexane to cyclohexane hydroperoxide
• olefins to epoxides such as ethene to ethylene oxide
• carbohydrates such as cyclohexane to cyclohexanol or cyclohexanone, toluene to benzaldehyde or benzoic acid, o-, m- or p-
• Oxidation of cyclohexane to a mixture containing cyclohexanol and cyclohexanone in the liquid phase with air in the presence of manganese is described as a technically significant oxidation in: Weissermel / Arpe, Industrielle Organische Chemie, 4th edition, VCH, Weinheim, 1994, page 260 ff. or cobalt salts as a catalyst at 125-165 ° C and a pressure in the range of 8 to 15 bar (absolute).
• the cyclohexane conversion is limited in order to achieve a selectivity that is technically meaningful. According to: Arpentier et al. , The Technology of Catalytic Oxidations, Editions Technip 2001, page 226 ff.
• the selectivity for cyclohexane conversions is in the range of 1-2% approx. 90%, while it is already for conversions from 4-5% to 77-85% waste.
• the unreacted cyclohexane must be distilled off in a downstream distillation column and returned to the oxidation stage.
• Cvclohexanol and cyclohexanone are starting materials for the production of caprolactam and adipic acid, both of which in turn are used to a considerable extent as monomers for the production of technically important polyamides.
• DE 19811517 describes the uncatalyzed, selective oxidation of cyclohexane with ozone to cyclohexanone in a reactor which is rendered inert to ozone, the ozone being metered in via the top of the column, while at the same time the cyclohexanone formed is continuously removed as product in the bottom of the column.
• Ozone is gaseous at technically relevant pressures and thus leaves the reactor again without sufficient contact with the hydrocarbon to be oxidized.
• the process should be carried out at temperatures less than or equal to the boiling point of the cyclohexane to be oxidized.
• the reaction products boil approx. 75 ° C higher than the starting material and the boiling point of the reaction mixture is above the boiling point of cyclohexane, this process is used for pure liquid phase conversion without distillation.
• This process therefore has the disadvantages already mentioned with regard to the separation of the reaction mixture and recycling of the cyclohexane.
• the object of the present invention was to provide a process which enables the oxidation of a, in particular organic, starting material with an oxidizing agent to obtain a product in a technically simple and economical manner while avoiding the disadvantages mentioned.
• the present process is suitable for the oxidation of a starting material.
• Inorganic, preferably organic compounds are suitable as starting materials.
• Unsaturated, preferably saturated hydrocarbons can be used as organic compounds.
• these hydrocarbons one or more carbon atoms can be replaced by heteroatoms, such as oxygen, nitrogen, sulfur, phosphorus, with the saturation of any free valences of such heteroatoms by hydrogen or substituents, in particular by the substituents mentioned below for the hydrocarbons; preferably no carbon atoms are replaced by such heteroatoms.
• the hydrocarbons with and without such heteroatoms are collectively referred to as hydrocarbons.
• Suitable unsaturated hydrocarbons are those with one or more triple bonds, one or more olefinic double bonds or aromatic systems or those which carry combinations of such features, such as ethene,
• Suitable unsaturated hydrocarbons can be linear or cyclic.
• Linear or preferably cyclic alkanes in particular having 2 to 12 carbon atoms, can be used as saturated hydrocarbons.
• Advantageous linear alkanes are ⁇ thane, propane, n-3utane, i-
• Cyclohexane or decalin can be used as cyclic alkanes.
• the process according to the invention can be applied to the oxidation of hydrocarbons or aldehydes to hydroperoxides, which can be used, for example, in the indirect epoxidation of olefins, such as acetaldehyde to peracetic acid, isobutane to isobutyl peroxide, isopentane to isopentyl peroxide, ethylbenzene to phenylethyl peroxide, cumene to be applied to cumene hydroperoxide, tetralin to tetralin hydroperoxide.
• olefins such as acetaldehyde to peracetic acid, isobutane to isobutyl peroxide, isopentane to isopentyl peroxide, ethylbenzene to phenylethyl peroxide, cumene to be applied to cumene hydroperoxide, tetralin to tetralin hydroperoxide
• the process according to the invention is capable of oxidizing hydrocarbons or aldehydes to acids or their anhydrides or their esters, such as p-xylene to terephthalic acid, m-xylene to isophthalic acid, o-xylene to phthalic acid or phthalic anhydride, and n-butane Acetic acid, toluene to benzaldehyde or benzoic acid, paraffins to acids, acetaldehyde to acetic acid, trimethylbenzene to hemimellitic acid, n-butyraldehyde to n-butyric acid, crotonaldehyde to crotonic acid, butane to ethyl acetate, butene to maleic anhydride, butane to maleic anhydride Maleic anhydride Maleic anhydride, propene to be applied to acrylic acid.
• hydrocarbons or aldehydes to acids or their anhydrides or their esters, such
• the process according to the invention can be used for the oxidation of hydrocarbons or aldehydes to ketones, alcohols or quinones, such as fluorene to fluorenone, trimethylphenol to trimethylquinone, acetaldehyde to acetic anhydride, naphthalene to naphthoquinone, anthracene to anthraquinone, p-diisopropylbenzene Hydroquinone, p-methylisopropylbenzene to cresol, paraffins to alcohols can be used.
• hydrocarbons or aldehydes to ketones, alcohols or quinones
• ketones such as fluorene to fluorenone, trimethylphenol to trimethylquinone, acetaldehyde to acetic anhydride, naphthalene to naphthoquinone, anthracene to anthraquinone, p-diisopropylbenzene Hydroquinone,
• the process according to the invention can be applied to the oxidation of alcohols to aldehydes or ketones, such as isopropanol to acetone, s-butanol to methyl ethyl ketone, methanol to formaldehyde.
• aldehydes or ketones such as isopropanol to acetone, s-butanol to methyl ethyl ketone, methanol to formaldehyde.
• the process according to the invention can be applied to the oxidation of CC single bonds to CC multiple bonds, such as butene to butadiene, ethyl benzene to styrene, methylcyclohexane to toluene, propane to propene can be used.
• the process according to the invention can be applied to the oxidation of hydrocarbons to nitriles, such as oxidation of toluene with N 2 O to benzonitrile.
• the method according to the invention can be applied to the oxidation of C-C single bonds or C-C multiple bonds by means of ozone while maintaining an acid function, such as the ozonolysis of native products to fatty acids.
• the process according to the invention can be applied to the oxidation of C-C multiple bonds by means of hydrogen peroxide to give the corresponding diols, such as allyl alcohol, to glycerol.
• the hydrocarbons can be used as a single compound or as a mixture of such hydrocarbons.
• cyclohexane can be used as the starting material.
• cyclohexanol, cyclohexanone, cyclohexyl hydroperoxide or their mixtures are advantageously considered as products.
• an educt is oxidized with an oxidizing agent.
• a gas containing molecular oxygen in particular molecular oxygen, can be used as the oxidizing agent.
• Molecular oxygen can be di-oxygen in the triplet or singlet form or tri-oxygen, that is to say ozone, preferably di-oxygen, in particular in the triplet form, or mixtures of such molecular oxygen forms.
• the gas containing such molecular oxygen can be free of further constituents.
• the gas containing such molecular oxygen can contain other, other constituents.
• constituents are gases having an oxidizing effect, such as nitrogen oxides
• other constituents advantageously inert gases, that is to say those which do not or not significantly enter into the oxidation reaction in the process according to the invention, can be used, such as nitrogen, for example in the form of air, or noble gases, for example argon, or their mixtures.
• a gas containing one or more nitrogen oxides, in particular one or more nitrogen oxides can be used as the oxidizing agent.
• Nitrogen oxides nitrogen monoxide, nitrogen dioxide or their mixtures or oligomers are suitable as nitrogen oxides.
• the gas containing one or more such nitrogen oxides can be free of further constituents.
• the gas containing one or more such nitrogen oxides can contain further, other constituents.
• gases which have an oxidizing action such as oxygen.
• inert gases that is to say those which do not or not significantly enter into the oxidation reaction in the process according to the invention, such as nitrogen, for example in the form of air, or noble gases, for example argon, or their mixtures.
• the oxidizing agent used can be a compound which is liquid under the reaction conditions, such as peroxides, for example inorganic peroxides, such as hydrogen peroxide, or organic peroxides, such as cyclohexane hydroperoxide, isobutyl hydroperoxide, isopentyl hydroperoxide, phenylethyl hydroperoxide, cumene hydroperoxide, tetralin hydroperoxide, oxide like peracetic acid.
• peroxides for example inorganic peroxides, such as hydrogen peroxide, or organic peroxides, such as cyclohexane hydroperoxide, isobutyl hydroperoxide, isopentyl hydroperoxide, phenylethyl hydroperoxide, cumene hydroperoxide, tetralin hydroperoxide, oxide like peracetic acid.
• the quantitative ratio between the starting material used and the molecular oxygen in the gas containing molecular oxygen depends on the desired degree of conversion of the starting material to the product from a chemical point of view, for example the conversion of an alkane to an alcohol or a ketone, and from a process engineering point of view, that is selected sales, and can easily be optimized by a few simple preliminary tests.
• Oxidizing agent and starting material can be added to the reaction device separately. Oxidizing agent and starting material can be partially mixed before addition to the reaction device and added to the reaction device.
• Oxidizing agent and starting material can be completely mixed before the addition to the reaction device and added to the reaction device.
• the oxidation is carried out in a reaction device which
• Rectification columns such as those described in: Kirk-Othmer, Encyclopedia of Chemical Technology, 3rd Ed., Vol. 7, John Wiley & Sons, New York, 1979, pages 870-881, are suitable as the preferred reaction device, such as tray columns , for example sieve plate columns or bubble plate plate columns, packing columns or packed columns.
• those trays are considered which enable a long residence time of the reaction mixture in the column, such as valve trays, preferably bubble trays or tunnel trays.
• packs such as metal mesh packs, sheet metal packs, advantageously with an ordered structure, or packings are suitable.
• accumulation packs come into consideration. Such accumulation packs allow the residence time in the reaction zone to be set on the basis of the pressure drop and ensure good separation performance even under high loads.
• internals with a high number of separating stages such as metal mesh packs or sheet metal packs, advantageously with an ordered structure, can be used in the reaction device below the lowest addition parts for the oxidizing agent.
• the rectification column should advantageously have a separation capacity of 10 to 100, preferably 20 to 40 theoretical plates.
• Feed oxidizing agent of the higher boiling reactant predominantly or completely above the lower boiling reactant to the reaction apparatus, in particular the higher boiling reactants can be fed into the upper part of the rectification column and the lower boiling reactants into the lower part of the rectification column.
• the higher boiling reactant can contain lower boiling reactants.
• the lower boiling reactant can contain higher boiling reactants.
• the rectification column has a distillation section between the reaction section and the bottom.
• reaction zone It has proven to be particularly advantageous to install 0 to 50, preferably 5 to 30, theoretical plates in the upper part of the rectification column, that is to say the reaction zone.
• the reaction zone can be located within the rectification section of the column.
• the reaction zone can be located outside the rectification section of the column.
• the reaction zone can be located outside the rectification column.
• the pressure in the reaction zone and the pressure in the rectification column can be the same or different.
• Fig. 1 shows schematically an advantageous embodiment of a reaction device. 1 mean:
• the process according to the invention can preferably be carried out in a plurality of reaction devices connected in series.
• the downstream reaction devices are operated at a lower pressure, part of the energy contained in the vapor stream of the front column can advantageously be transferred to the feed stream of one of the downstream reaction devices.
• part of the uncondensed vapor stream can advantageously be returned to the lower part of the reaction device.
• This cycle gas mode of operation makes it possible to recover part of the energy present in the bottom stream.
• the average residence time of the reaction mixture on the trays of the column should be 1 to 120 minutes, preferably 5 to 30 minutes.
• the process according to the invention can advantageously be carried out, in particular in the case of cyclohexane as starting material, at a pressure in the range from 0.1 to 3.5 MPa, preferably from 0.5 to 2.5 MPa, measured in the bottom region of the reaction device.
• the temperature is then considered such that the reaction mixture in the reaction zone is kept in the boiling state.
• the temperature suitable for the respective implementation can easily be determined by a few simple preliminary tests.
• temperatures in the range from 70 to 220 ° C., preferably from 120 to 190 ° C., are advantageous in the reaction zone.
• the reaction device at the upper end of the head part can have a possibility for the removal of gases.
• the reaction is advantageously carried out in such a way that the reaction mixture present there below the reaction zone evaporates to give a mixture of liquid and gaseous reaction mixture.
• the reaction device in the bottom region and in the region of the reaction zone is filled with a liquid reaction mixture.
• the gaseous reaction mixture obtained in this way then increases due to the lower density compared to the liquid reaction mixture in the direction of the head region of the reaction device. Due to the interaction between the gaseous and the liquid phase, changes in the composition of the gas phase can occur due to condensation and evaporation processes.
• the gaseous reaction mixture arriving there is condensed in the head region of the reaction device and thus fed to the reaction zone, advantageously in the liquid phase.
• the oxidizing agent is brought into the reaction zone in at least 2, preferably 2 to 100, in particular 2 to 50, particularly preferably 2 to 40, such as 2, 3, 4, 5, 6, 7, 8, 9, 10, 11, 12 , 13, 14, 15, 16, 17, 18, 19, 20 partial flows.
• the oxidizing agent can be introduced into the reaction device according to methods known per se, in particular for introducing a gas into a liquid.
• the process according to the invention can be carried out without a catalyst.
• the process according to the invention can be carried out in the presence of a homogeneous or heterogeneous catalyst.
• a homogeneous catalyst it can advantageously be added to the reaction mixture in the top area of the reaction device and removed with the reaction mixture in the bottom area. If a heterogeneous catalyst is used, it can advantageously be fixed in the reaction zone of the reaction device by methods known per se.
• the catalysts known per se for the respective oxidation reactions can be used, for example in the case of the oxidation of cyclohexane to cyclohexanol, cyclohexanone or their mixtures containing salts containing cobalt or manganese.
• the amounts of catalyst can easily be determined in accordance with the catalyst loads known for these catalysts for the respective reactions and the conversions selected in the process according to the invention, and the catalyst amounts can be easily optimized by means of a few simple preliminary tests.
• a reaction mixture containing the product can advantageously be removed in the bottom region of the reaction device, in particular if the boiling point of the product is higher than the boiling point of the starting material under the reaction conditions.
• the reaction mixture withdrawn at the bottom can consist of product or a mixture which contains the product along with other components, such as starting material, by-products, secondary products.
• a reaction mixture containing the product can advantageously be removed in the top region of the reaction device, in particular if the boiling point of the product is lower than the boiling point of the starting material under the reaction conditions.
• the reaction mixture removed in the top region can consist of product or a mixture which contains the product along with other components, such as starting material, by-products, secondary products.
• the cyclohexane stream which was added at the top of the reactor was adjusted so that the residence time of the liquid phase in the reactor was 31 minutes.
• By adding an appropriate amount of air was evenly distributed over the chambers of the reactor set a cyclohexane conversion of 3.5%.
• the reactor was operated at a pressure of 16 bar.
• the selectivity to cyclohexanol, cyclohexanone and cyclohexane hydroperoxide was 83.9% in total.
• the space-time yield based on the liquid phase in the reactor was 45.7 kg / (m 3 * h).
• a reaction column with 10 stages in the reaction part (top) and 10 stages in the distillation part (bottom) was fed 2415 kg / (m 3 * h) of cyclohexane above the reaction part, based on the liquid phase volume.
• the column was operated at a pressure of 11.9 bar. 0.15 Nm 3 of air per kg of cyclohexane were distributed uniformly over the 10 stages of the reaction part of the column. With an evaporator energy of 200 Wh / kg based on the fresh cyclohexane stream, the cyclohexane conversion was 10.1%.
• the selectivity to cyclohexanol, cyclohexanone and cyclohexane hydroperoxide was 88.0% in total.
• the space-time yield based on the liquid phase in the reactor was 250 kg / (m J, r h).
• the selectivity to cyclohexanol, cyclohexanone and cyclohexane hydroperoxide was 84.1% in total.
• the space-time yield, based on the remplissigphas * e in the reactor was 232 kg / (m 3 ⁇ h).

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• Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
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• 2002
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• 2003
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  • 2003-07-30 JP JP2004531837A patent/JP2005536341A/ja active Pending
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  • 2003-07-30 WO PCT/EP2003/008407 patent/WO2004020083A1/de active Application Filing
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