EP2547670A1 - Procédé d'oxydation catalytique d'hydrocarbures en phase gazeuse et réacteur de catalyse - Google Patents

Procédé d'oxydation catalytique d'hydrocarbures en phase gazeuse et réacteur de catalyse

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Publication number
EP2547670A1
EP2547670A1 EP11709121A EP11709121A EP2547670A1 EP 2547670 A1 EP2547670 A1 EP 2547670A1 EP 11709121 A EP11709121 A EP 11709121A EP 11709121 A EP11709121 A EP 11709121A EP 2547670 A1 EP2547670 A1 EP 2547670A1
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EP
European Patent Office
Prior art keywords
reaction
catalyst
coolant
gas
temperature
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.)
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Application number
EP11709121A
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German (de)
English (en)
Inventor
Gerhard Mestl
Hans-Jörg WÖLK
Sebastian KNEIßL
Christoph BÄUMLER
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.)
Sued Chemie IP GmbH and Co KG
Original Assignee
Sued Chemie IP GmbH and Co KG
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Publication date
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Publication of EP2547670A1 publication Critical patent/EP2547670A1/fr
Withdrawn legal-status Critical Current

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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
    • C07C51/255—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
    • 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
    • C07C51/31—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation of cyclic compounds with ring-splitting
    • C07C51/313—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation of cyclic compounds with ring-splitting with molecular oxygen
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07D—HETEROCYCLIC COMPOUNDS
    • C07D307/00—Heterocyclic compounds containing five-membered rings having one oxygen atom as the only ring hetero atom
    • C07D307/77—Heterocyclic compounds containing five-membered rings having one oxygen atom as the only ring hetero atom ortho- or peri-condensed with carbocyclic rings or ring systems
    • C07D307/87—Benzo [c] furans; Hydrogenated benzo [c] furans
    • C07D307/89—Benzo [c] furans; Hydrogenated benzo [c] furans with two oxygen atoms directly attached in positions 1 and 3

Definitions

  • the present invention relates to a method for
  • a suitable catalyst for this reaction in a reactor preferably a so-called tube bundle reactor in which a plurality of tubes is arranged in parallel, filled, which subsequently with a reaction mixture of o-xylene and / or naphthalene and an oxygen-containing gas, such as For example, air is flowed through. Due to the strong heat generation of such oxidation reactions it is necessary to surround the reaction tubes to avoid so-called "hotspots" with a heat transfer medium and dissipate the resulting heat energy, the
  • the heat transfer medium used is usually a molten salt, and preferably a eutectic mixture of a 0 2 and KNO3.
  • Phthalic anhydride by providing a
  • Catalyst moldings or supported catalysts can be achieved. Systems with several catalyst layers are described, for example, in WO 2006/125467 or WO 2006/125468
  • Catalyst layers after their arrangement in a catalytic device can not be changed or only in a laborious manner.
  • Another approach to improving the performance of a process for the catalytic gas phase oxidation of hydrocarbons is based on two or more
  • the object of the present invention was therefore to develop a process for the catalytic gas-phase oxidation of hydrocarbons, which contributes to the disadvantages of known
  • the process should be designed such that the catalyst system used in the process also during the
  • a process for the catalytic gas-phase oxidation of hydrocarbons comprising the steps of a) providing a catalytic reaction device with a cooled with refrigerant reaction space between a gas inlet and a gas outlet and a catalyst bed b) conducting a hydrocarbon-containing
  • the gas flow direction can be any gas flow direction.
  • reaction space is designed so that it has one or more reaction zones, which may also be spatially separated from each other.
  • reaction zone describes one or more sections or one or more elements of the catalytic reaction device or the associated reaction space, in which one or more catalyst (s) or one or more combinations of catalysts, for example in the form of a
  • Catalyst layers is present or present, through which the
  • a reaction zone comprises a portion of a catalyst bed.
  • catalyst bed refers to a plurality of individual catalysts, i. supported catalysts or
  • the first, the second and the at least one further reaction zone lie in the same element of the catalytic converter
  • first reaction zone, the second reaction zone and the at least one further reaction zone in separate elements of the catalytic reaction apparatus, for example in separate reactors, such as a main and a post-reactor (finishing reactor) or in a Are upstream and a main reactor, or in particular present in separate catalyst beds.
  • the length of a reaction zone is at least 1/30, more preferably at least 1/16, of the total bed length of the catalysis reaction device filled with one or more catalyst (s).
  • the length of a reaction zone is at least 1/30, more preferably at least 1/16, of the length of a catalyst bed filled with one or more catalyst (s) in the catalytic reaction apparatus.
  • the respective reaction zones may be the same length or different lengths.
  • reaction zone through which the reaction mixture is passed after passing through the first reaction zone is referred to as the second reaction zone.
  • the reaction zone passed through after the second reaction zone becomes third
  • Coolant manages the content of undesirable
  • catalytic gas phase oxidation of hydrocarbons comprises first the step of providing a
  • a catalytic reaction apparatus comprising, in succession with respect to the gas flow direction, a first reaction zone cooled with coolant, a second reaction zone cooled with coolant and at least one further reaction zone cooled with coolant.
  • Process according to the invention can also be carried out only with 2 of the reaction zones described above.
  • the inventive method thus includes according to this
  • Embodiment a) providing a A catalytic reaction apparatus comprising, in sequence with respect to the gas flow direction, a first reaction zone cooled with coolant, a second reaction zone cooled with coolant, and at least one further reaction zone cooled with coolant, and
  • catalyst reaction device includes any device known to those skilled in the art, comprising one or more catalyst (s) or combination (s) of catalysts in which catalytic gas phase oxidation can be performed.
  • Catalyst reaction apparatus may, for example, comprise one or more reactors, for example, pre-, main and / or post-reactors.
  • reactors for example, pre-, main and / or post-reactors.
  • Catalytic reaction apparatus for example, one or more catalyst bed (s) (called catalyst layers) in a catalyst bed comprising one or more catalyst (s) or one or more combination (s) of catalysts, wherein the one or multiple catalyst (s) or the one or more combinations of catalysts may be the same or different.
  • a catalytic reaction device may comprise devices known to those skilled in the art for supplying and / or producing and / or mixing reaction mixtures, in particular gaseous reaction mixtures.
  • reactors can be used, as described in WO 2006/069694, the disclosure of which hereby is fully incorporated in the present application.
  • the method can be carried out particularly advantageously in a device with thermoplates, wherein a
  • Reaction mixture and / or an optional post-reactor are arranged in the same device.
  • Reaction mixture and / or an optional post-reactor are arranged in the same device.
  • Coolant for example along at least one
  • Section of the wall of a reaction zone limiting elements can in principle be carried out in any manner known to a person skilled in the art.
  • the catalysts may, for example, with regard to the composition of the
  • Active composition in particular with regard to the amount and the selection of catalytically active metals and / or promoters, the BET surface area characteristic, the pore size, the
  • a combination of catalysts are multiple layers of at least partially different catalysts or mixtures of catalysts.
  • the catalytic gas phase oxidation of hydrocarbons may be accomplished using any catalyst or combination of catalysts that is useful for the catalytic gas phase oxidation of hydrocarbons in the presence of an oxidizing agent, particularly gaseous oxygen, can be used. such
  • Catalysts or combinations of catalysts are known to those skilled in the art and can be selected based on the general knowledge and teaching of the present invention.
  • Catalyst systems used are: oxidation of
  • promoted MoVW mixed oxide catalysts oxidation of propane to acrylic acid via promoted MoVNbTe mixed oxide catalysts, oxidation of n-butene to maleic anhydride via promoted VPO catalysts, oxidation of i-butene via promoted BiMo mixed oxide catalysts to methacrolein, oxidation of methacrolein via promoted heteropolyacid or
  • Reaction mixture may include oxygen or at one be mixed with oxygen or come into contact with it at any point before or during the passage through the first reaction zone.
  • the reaction mixture can at
  • Reaction mixture that is, for example, as a
  • Reaction mixture at least from the entrance to the first
  • Reaction zone as a gaseous reaction mixture before.
  • reaction mixture can comprise any carrier substances known to a person skilled in the art, in particular carrier gases, suitable reaction moderators and / or diluents such as steam, carbon dioxide and / or nitrogen.
  • carrier gases such as steam, carbon dioxide and / or nitrogen.
  • suitable reaction moderators such as steam, carbon dioxide and / or nitrogen.
  • a molecular oxygen-containing gas may be mixed with o-xylene and / or naphthalene, which is generally 1 mol% to 100 mol%, preferably 2 mol% to 50 mol% and especially
  • reaction gas preferably 10 mol% to 30 mol% oxygen, 0 to 30 mol%, preferably 0 to 10 mol% water vapor and 0 to 50 mol%, preferably 0 to 1 mol% carbon dioxide, balance nitrogen.
  • Hydrocarbon are fed.
  • the method of the invention comprises passing the hydrocarbon-containing reaction mixture through the catalytic reaction device in the gas flow direction through the first coolant cooled reaction zone, the second coolant cooled reaction zone, and the at least one further with coolant cooled reaction zone.
  • the first and second reaction zones may preferably follow one another directly and / or adjoin one another. However, the first and second reaction zones may be spaced apart from each other,
  • Catalyst reaction apparatus comprising no catalyst or inert material, such as through a pipe or
  • Catalyst bed or more catalyst beds are catalyst beds. The same applies to the other existing reaction zones.
  • Reaction zone and the at least one further reaction zone optionally by further catalytic reaction devices and devices for purification, further treatment or
  • the temperature profile of the coolant is a discontinuously increasing temperature profile.
  • discontinuous increase in the temperature profile can be realized, for example, so that the increase in the coolant temperature profile between two
  • the process can be discontinuous Temperature profile be designed so that the
  • Reaction space sequentially in the gas flow direction has at least two temperature zones of different temperature.
  • the reaction space has at least two reaction zones, the
  • Temperature zones can correlate with the reaction zones.
  • the temperature profile is a continuously increasing temperature profile, which is technically easy and cheap to implement.
  • the method according to the invention is the increasing
  • catalytic gas-phase oxidation of hydrocarbons can be obtained when the temperature of the coolant and thus the reaction temperature variable to the course of the respective plant conditions, in particular to the age of the catalyst and operational changes,
  • Temperature profile i. the rising temperature profile to change.
  • a first reaction period which may be, for example, min. 400 hours, preferably 365 days persists
  • another Temperature profile can be selected, ie, it can compared to the first reaction period another temperature for the first reaction zone cooling coolant and / or the second reaction zone and / or the at least one further reaction zone cooling coolant in contact with the
  • respective reaction zone can be selected.
  • Temperature of the coolant cooling the first reaction zone and / or the temperature of the coolant cooling the second reaction zone and / or the temperature of the coolant cooling the at least one further reaction zone and / or the position of at least one reaction zone can be changed.
  • any reaction zones coolant during a second reaction period by, for example, at least 2 ° C, preferably at least 5 ° C, preferably at least 15 ° C, more preferably at least 30 ° C be increased or decreased, but without the temperature profile of the invention, ie the rising temperature profile to change.
  • the position of the first, the second or the at least one further reaction zone can optionally be changed during a second reaction period.
  • a reaction zone can be increased or decreased. This can be done, for example, by the route corresponding to a particular reaction zone is chosen to be longer or shorter along a catalyst bed or catalyst bed.
  • the catalysis reaction device is equipped with one or more devices that allow the position of the first reaction zone, the second reaction zone, or optionally other reaction zones to be changed, such as e.g. adjustable baffles, in particular in or on a reactor tube casing, the variable deflection of a coolant flow or more
  • Reaction zone (s) take place.
  • Catalyst can be counteracted.
  • deactivation of the main catalyst layer ie, the catalyst layer which has a hotspot or also further layers, occurs, for example, the hotspot temperature decreasing, the hotspot position falling into deeper zones, For example, it also shifts to other locations and widens the hot spot, which can be deactivated during the life cycle of the catalyst
  • the control of the temperature of a coolant can be by any known in the art methods and
  • control may be provided by one or more cooling and / or heating devices that are responsive to one or more temperature sensing devices that sense the temperature of a temperature sensing device
  • Temperature range can optionally be determined by simple experiments. Particularly advantageous results, in particular with regard to a simple implementation of the invention
  • the coolant is a salt or a salt mixture.
  • eutectic salt mixtures such as a eutectic mixture of a 0 2 and KNO 3, may be suitable as a coolant.
  • coolant for example, water,
  • Diphyl ® (a mixture of 70 wt .-% to 75 wt .-% of diphenyl ether and 25 wt .-% to 30 wt .-% diphenyl, available from LANXESS Germany GmbH) or ionic liquids as
  • ionic liquids containing sulfate, phosphate, borate or silicate anions.
  • ionic liquids which contain a monovalent metal cation, in particular an alkali metal cation, and also a further cation, in particular an imidazolium cation,
  • ionic liquids containing as cation an imidazolium, pyridinium or phosphonium cation are also advantageous.
  • Reaction zone can be the same coolant or
  • Reaction zones be provided with a separate coolant circuit.
  • the process according to the invention is a process for the preparation of phthalic anhydride in which the
  • Reaction mixture to obtain a particularly low content of unreacted organic starting materials and a particularly low content of the by-product
  • Reaction mixture has a content of o-xylene and / or naphthalene of less than 0.3 wt .-%, preferably less than 0.2% by weight and in particular less than 0.1 wt .-%, and a
  • Hydrocarbons in the reaction mixture have.
  • a hydrocarbon is any compound which comprises at least one carbon atom and at least one hydrogen atom.
  • the temperature of the gas outlet or the Cooling agent last cooling reaction zone by 5 ° C to 35 ° C higher than the temperature of the cooling at the gas inlet or the first reaction zone coolant.
  • the temperature of the cooling of the last reaction zone coolant is higher by 10 ° C to 30 ° C, preferably by 15 ° C to 25 ° C higher than the temperature of the coolant cooling the first reaction zone.
  • Gas inlet or the first reaction zone cooling coolant in a range of 270 ° C to 360 ° C and the temperature of the gas outlet or the last reaction zone cooling
  • Coolant in a range of 275 ° C to 395 ° C.
  • Cooling reaction zone in a range from 290 ° C to 340 ° C, preferably from 300 ° C to 375 ° C, and the
  • the reaction space comprises successively between the gas inlet and the gas outlet and / or in the gas flow direction at least two catalyst layers, wherein the catalyst layers have a catalytic activity profile, which is equal or increased in the gas flow direction.
  • the reaction zones each comprise at least one catalyst layer, wherein the catalyst layers per reaction zone have a catalytic activity profile which in the
  • Catalyst layers the catalytic activity profile in
  • Gas flow direction is preferably the same, with more than two catalyst layers, the catalytic activity profiles are either ascending in the gas flow direction, i. always higher, or equal between the first and second catalyst layer and ascending from the third catalyst layer.
  • the catalytic takes
  • Activity profile in the gas flow direction between the first and second catalyst layer first off and increases from the third again.
  • Coolant is rising in the gas flow direction and in particular the temperature of the gas outlet or the last reaction zone cooling coolant by 5 ° C to 35 ° C is higher than the temperature of the gas inlet or the first
  • catalyst layers in the reaction space or in the reaction zones, can be used which have a catalytic activity profile which is the same and / or ascending in the gas flow direction (see also the above explanations)
  • the different catalytic activity in the respective catalyst layers is adjusted by
  • the geometric shape of the catalyst body in particular in the case of supported catalysts or
  • Supported catalysts for example, influence on the bulk density of the catalyst in a
  • Reactor tube or the surface or the dynamic pressure has.
  • chemical properties for example
  • compositions presence of various promoters and the like of the catalysts are understood.
  • Catalyst layer of the second reaction zone can be achieved by a lower content of active mass than in the catalyst layer of the first reaction zone, by a lower BET surface area of a carrier oxide for the catalytically active mass than in the catalyst layer of the first reaction zone, by a lower content of catalytically active
  • Catalyst layer of the first reaction zone by a Reduction of the bulk density in the catalyst layer of the second reaction zone, for example by using a different geometry or ring geometry of the used
  • the catalyst layer of the second reaction zone compared to the catalyst layer of the first reaction zone has a lower active material content, and / or a lower BET surface, and / or a lower content of damping promoters. Since the BET surface area of the catalyst layer depends primarily on the BET surface area of the carrier oxide used, according to a preferred invention
  • the BET surface area of the carrier oxide in the catalyst layer of the second reaction zone less than the BET surface area of the carrier oxide in the catalyst layer of the first reaction zone.
  • the activity of the preceding catalyst layer is at least 5%, in particular at least 10%, preferably at least 20%, particularly preferably at least 30% lower than the activity of the subsequent catalyst layer.
  • the activity of the catalyst layer is on
  • Embodiment of the invention 300% higher than that of the subsequent catalyst layer, z. B. the second
  • Reaction zone preferably at most 200%, more preferably at most 100% and particularly preferably at most 80% higher than the activity of the subsequent catalyst layer. Particularly good results are achieved when the activity of the
  • Catalyst layer at the gas inlet or the first reaction zone in the range of 5 to 30% higher than that of the subsequent catalyst layer, e.g. the second reaction zone.
  • Catalyst layers in a preferred embodiment of the method according to the invention comprise an inert support and a catalytically active material disposed thereon.
  • the catalytically active composition comprises in a further preferred
  • the catalytically active composition or the catalytically active composition contains as active component preferably vanadium, niobium, antimony, boron, calcium, cesium, potassium, lithium, sodium, cobalt, iron, molybdenum, zirconium, rubidium, silver, thallium, bismuth, tungsten, Tin, phosphorus and / or their compounds and / or combinations thereof.
  • the catalytically active composition particularly preferably contains vanadium as the active component,
  • Composition included.
  • the titanium-containing carrier oxide preferably has a BET surface area of 10 m 2 / g to 50 m 2 / g, particularly preferably 15 m 2 / g to 45 m 2 / g and especially about 20 m 2 / g to 35 m 2 / g.
  • the individual catalysts of the catalyst layers each contain at least titanium and preferably also vanadium in the catalytically active composition.
  • the individual catalyst layers preferably have no molybdenum and / or no tungsten, in particular not in an atomic state
  • the sodium content in the active composition is preferably less than 500 ppm, in particular less than 450 ppm.
  • the catalysts in the catalytically active composition comprise the following
  • V 2 O 5 in the range from 1% by weight to 25% by weight, preferably 4% by weight to 20% by weight
  • Sb 2 Ü 3 in the range from 0 to 4% by weight, preferably 0, 5 wt .-% to 3.5 wt .-%
  • cesium in the range of 0 - 1 wt .-%, preferably 0.1 wt .-% to 0.8 wt .-%
  • Catalyst is preferably 4 wt% to 20 wt%, more preferably 4 wt% to 15 wt%.
  • Active composition of at least 90% by weight, preferably at least 95% by weight, more preferably at least 98% by weight, in particular at least 99% by weight, more preferably 99.5% by weight,
  • the catalytic reaction apparatus has five reaction zones.
  • the fifth reaction zone is at the
  • Gas outlet side for example, at the gas outlet, the
  • Phthalic acid production it may also be possible to use a so-called finishing reactor, e.g. in DE-A-198 07 018 or DE-A-20 05 969 is described.
  • the catalyst layer at the gas inlet or the first reaction zone preferably has an active composition content of between about 7% by weight and 13 wt .-%, in particular between 7 wt .-% and 12 wt .-%
  • the catalyst layer of the second reaction zone preferably has an active composition content between about 6 wt .-% and 12 wt .-%
  • Catalyst layer of the third reaction zone preferably has an active material content of between about 5% by weight and 11% by weight,
  • Catalyst layer of the fourth reaction zone preferably has an active material content between about 4 wt .-% and 15 wt .-%,
  • Catalyst layer of the fifth reaction zone preferably has an active material content of between about 3% by weight and 18% by weight,
  • the active mass content of the individual reaction zones can be designed by a person skilled in the art in an analogous manner, ie. first sloping from the first to the second reaction zone, then increasing to the last
  • the BET surface area of the T1O 2 used decreases from that
  • Preferred ranges for the BET surface of the T1O 2 are 15 to 25 m 2 / g for the catalyst layers in the middle region of the
  • Reaction space for example, the middle reaction zones, and 15 to 45 m 2 / g for those to the gas outlet side located
  • Catalyst layer of the last reaction zone increases. According to another preferred invention
  • Embodiment will be at least 30%, in particular
  • Pore fractions unless otherwise stated, by means of mercury porosimetry (according to DIN 66133).
  • the indication of the total pore volume refers in the present description in each case to the entire means
  • Mercury porosimetry measured pore volume between 7500 and 3.7 nm pore radius size.
  • Pores having a radius greater than 400 nm are preferably less than about 30%, more preferably less than about 22%, most preferably less than 20% of the total
  • Pore volume of Ti0 2 used is a Pore volume of Ti0 2 used .
  • Pore volume can be formed by pores with a radius of more than 400 nm. With regard to the smaller pore radii, it is preferred that less than 30%, in particular less than 20%, of the total pore volume of the T 1 O 2 be formed by pores having a radius of 3.7 to 600 nm. A particularly preferred here
  • Range is about 10 to 30% of the total pore volume, in particular 12 to 20% for this pore size.
  • the T 1 O 2 used has the following particle size distribution: the Di o value is preferably 0.5 ym or less, the D 5 o value (ie the value at which each half of the particles larger or smaller particle diameter) is preferably 1.5 ym or less; the Dgo value is preferably 4 ym or less.
  • the D90 value of the T 1 O 2 used is between about 0.5 and 20 ⁇ m, in particular between about 1 and 10 ⁇ m, particularly preferably between about 2 and 5 ⁇ m.
  • T 1 O 2 used according to the invention preferably has an open-pore, sponge-like structure, with primary particles or
  • Crystalline to more than 30%, in particular more than 50%, are joined together to open-pore agglomerates. It is believed that by this particular structure of the
  • T 1 O 2 used which is reflected in the pore radius distribution, created particularly favorable reaction conditions for the gas phase oxidation.
  • Catalysts also another titanium oxide with another
  • Particle size distribution can be used. However, it is particularly preferred according to the invention that at least 50%, especially at least 75%, most preferably the total TiO 2 used , a BET surface and porosimetry as defined herein, and preferably also the one described
  • the components known and customary to those skilled in the art may be contained in the active composition of the catalyst.
  • the form of the catalyst or its homogeneous or heterogeneous structure is in principle not limited in the meaning of the present invention and can be any of those skilled in the art and appear suitable for the respective process
  • Embodiment include.
  • an inert under the reaction conditions carrier for example, quartz (Si0 2 ), porcelain, magnesium oxide, tin dioxide, silicon carbide, rutile, alumina (Al 2 O 3 ),
  • the carrier may, for example, have the form of rings, balls, shells or hollow cylinders.
  • the catalytically active material is applied in relatively thin layers (shells). It is also possible to apply two or more layers of the same catalytically active composition or differently composed catalytically active compositions.
  • the compositions described in the relevant prior art and familiar to the person skilled in the art or components are referenced. These are mainly catalyst systems which contain oxides of vanadium in addition to titanium oxide (s). Such catalysts are described, for example, in EP 0 964 744 B1.
  • a very small particle size V ⁇ Os material is used to favor deposition on the T1O 2 .
  • at least 90% of the V ⁇ Os particles employed may have a diameter of 20 ym or less.
  • Promoters for increasing the productivity of the catalysts described which can also be used in the catalyst according to the invention. These include u.a. the alkali and alkaline earth metals, thallium, antimony, phosphorus, iron, niobium, cobalt, molybdenum, silver, tungsten, tin, lead and / or bismuth and mixtures of two or more of the above components.
  • Catalysts used according to the invention thus one or more of the above promoters.
  • a catalyst is described in DE 21 59 441 A, in addition to
  • Titanium dioxide of anatase modification from 1 to 30% by weight
  • Vanadium pentoxide and zirconium dioxide An enumeration of suitable promoters can also be found in WO 2004/103561, page 5, lines 29 to 37, to which reference is also made. Via the individual promoters, the activity and selectivity of the catalysts can be influenced, in particular by lowering or increasing the activity. To the the the the individual promoters
  • Selectivity controlling promoters include, for example, the alkali metal oxides and oxidic phosphorus compounds,
  • the phosphorus pentoxide in particular phosphorus pentoxide.
  • the phosphorus pentoxide in particular phosphorus pentoxide.
  • Activity can be achieved, wherein the selectivity in the catalyst layers of the following sections (e.g., third and subsequent reaction zone (s)) e.g. by the presence of
  • Phosphorus compounds can be advantageously adjusted. In some cases, it may be advantageous if only the last layer has a phosphorus compound.
  • suitable processes are described in the prior art.
  • For the preparation of coated catalysts reference may be made, for example, to the process described in DE-A-16 42 938 or DE-A-17 69 998, in which one containing an aqueous and / or an organic solvent
  • heated coating drum is sprayed at elevated temperature until the desired content of catalytically active composition, based on the total weight of the catalyst, is reached. Also, according to DE 21 06 796 the application
  • So-called shell catalysts are preferred by the application of a thin layer of 50 to 500 ym of
  • Active components prepared on an inert support eg US 2,035,606
  • a carrier in particular balls or Hollow cylinder proven.
  • the sintered moldings must be inside the
  • Temperature range of the ongoing reaction to be heat resistant As stated above, in this case, for example, silicon carbide, steatite, quartz, porcelain, Si0 2 , I 2 O 3 or alumina in question.
  • the advantage of coating carrier bodies in the fluidized bed is the high uniformity of the layer thickness, which plays a decisive role for the catalytic performance of the catalyst.
  • a particularly uniform coating is obtained by spraying a suspension or solution of
  • Active components on the heated support at 80 to 200 ° C in a fluidized bed for example according to DE 12 80 756, DE 198 28 583 or DE 197 09 589.
  • Active components on the heated support at 80 to 200 ° C in a fluidized bed for example according to DE 12 80 756, DE 198 28 583 or DE 197 09 589.
  • Drag drums can also use the.
  • hollow cylinders as a carrier in said fluidized bed process
  • the method according to DE 197 09 589 is of particular advantage since, in addition to a uniform coating, a slight abrasion of parts of the apparatus is achieved by the predominantly horizontal, circular movement of the carrier.
  • Naphthalene are well known to those skilled in the art. In particular, reference is made to the summary in K. Towae, W. Enke, R. Jaeckh, N. Bhargana
  • the catalysts in the reaction tubes of the reactor which are thermostated from the outside to the reaction temperature, for example by means of molten salts, filled.
  • the reaction gas at temperatures of generally from 300 ° C to 450 ° C, preferably 320 ° C to 420 ° C, and especially
  • the reaction gas supplied to the catalyst is in
  • Reaction moderators and / or diluents such as vapor, carbon dioxide and / or nitrogen may contain, produced with the aromatic hydrocarbon to be oxidized, wherein the molecular oxygen-containing gas is generally 1 mol% to 100 mol%, preferably 2 mol% to 50 mol% and particularly preferably 10 mol% to 30 mol% oxygen, 0 to 30 mol%, preferably 0 to 10 mol% water vapor and 0 to 50 mol%, preferably 0 to 1 mol% carbon dioxide, rest
  • Nitrogen may contain.
  • the catalyst for at least 24 hours at least 390 ° C, especially between 24 and 72 hours at> 400 ° C, in a 02-containing gas, especially in air, with a flow rate per reaction tube of at least 0th , 1 Nm 3 / h, is calcined.
  • the temperature should preferably not exceed 500 ° C, especially 470 ° C. In principle, however, other calcination conditions which appear to the person skilled in the art are not excluded.
  • Another aspect of the present invention relates to a catalytic reaction apparatus for catalytic
  • reaction space between a gas inlet and a
  • catalytic activity profile that is equal or increasing from the gas inlet to the gas outlet. It can be one
  • Coolant means may be provided, which is designed such that the reaction space with a from the gas inlet to
  • the present invention provides, in another aspect, a catalytic reaction apparatus for the catalytic gas phase oxidation of hydrocarbons having, in sequence with the gas flow direction, a first coolant cooled reaction zone, a second coolant cooled reaction zone and at least one further coolant cooled reaction zone, wherein the reaction zones each comprise at least one catalyst layer, characterized in that the catalyst layers have a catalytic activity profile that is known in the
  • Catalyst layer drops and then increases again.
  • the catalytic reaction apparatus according to the invention can be used in the catalytic process described above
  • the proportion of active mass in each case relates to the proportion (in% by weight) of the catalytically active composition of the total weight of the catalyst, including carriers in the respective one
  • Catalyst layer measured after conditioning for 4 h at 400 ° C in air. 2. Determination of a coolant temperature or a coolant temperature difference
  • a detection of the temperature of the coolant upon contact with a reaction zone can be carried out by any method known to a person skilled in the art. If only the determination of the difference of the temperatures of different
  • Reaction zones for example, the first reaction zone or the second reaction zone
  • cooling coolant is required in contact with the respective reaction zones, in this case, only a detection of the temperature difference can take place.
  • a preferred detection of the temperature of the coolant can be carried out by a temperature detecting device, which determines the temperature of the coolant when in contact with the
  • thermocouple e.g. Type K
  • the BET surface area was determined by the BET method according to DIN 66131; a publication of the BET method can also be found in J. Am. Chem. Soc. 60, 309 (1938).
  • the information given in the present description with regard to the BET surface areas of the catalysts or catalyst layers relates to the BET surface areas of the respective TiO 2 material used (dried in vacuo at 250 ° C., uncalcined).
  • the BET surface area of the catalyst is determined by the BET surface area of the T1O 2 used , with the addition of further catalytically active components determining the BET surface area of the catalyst. Surface is changed to some extent. This is familiar to the expert.
  • Pore volume and the particle size distribution was carried out with respect to the titanium dioxide in each case at the dried at 250 ° C in a vacuum, uncalcined material.
  • the pore radius distribution of the T1O 2 used was determined by mercury porosimetry according to DIN 66133;
  • the sample is homogenized in deionized water without the aid of auxiliaries and sonicated for 5 minutes. 6. Catalyst activity
  • reaction tube of defined length and inner diameter (eg 25 mm inner diameter, 1 m length), at given reaction conditions (temperature, pressure, concentration, residence time) to implement the starting material used.
  • the considered catalyst accordingly has a higher Activity as another catalyst, if in this given volume and under the same one
  • the activity of the first layer is higher than that of the second layer.
  • Temperature cooling medium 380 - 420 ° C
  • the quantification of the activity of the first catalyst layer in comparison to the activity of the second catalyst layer can then be determined as follows from the following inventive definition of a "catalyst with 10% higher activity" used for layer 1 versus a catalyst used for layer 2:
  • Total volume flow through the reaction tube is adjusted so that the o-xylene conversion is as close as possible to 50% after flowing through the portion of the reaction space.
  • the same reaction volume is filled with layer 1 (test) catalyst, which differs from layer 2 catalyst only in that the proportion of the catalytically active material (active mass fraction) is, for example, 10% higher.
  • the reaction volume thus contains 10% more active mass than in the case of the comparative catalyst arrangement. It is then determined under the same reaction conditions of o-xylene conversion after flowing through the filled with layer 1 catalyst portion of the reaction chamber. This is higher than with the comparative catalyst, ie higher than 50%.
  • the difference between the thus obtained o-xylene conversion to the 50% conversion of the comparative catalyst is used as a relative measure corresponding to a 10% increase in activity. It is irrelevant, by which change in the catalyst, such an effect is achieved. Accordingly, for example, with a catalyst that differs from the intended location 2 catalyst only in that the Active mass fraction is 20% higher, a figure for a 20% increased activity of the catalyst can be determined etc.
  • the catalytic reaction apparatus used had 4
  • Reaction zones each having the catalyst layers and layer lengths defined in Table 1 below in one
  • reaction tube was centrally arranged a 3 mm thermal sleeve with built-in tension element for
  • V 2 0 5 / wt. -% 8, 0 7.5 7.5 7.5
  • Reaction tube passed through a gas chromatograph and an IR analyzer, with which all components of the
  • Reactive gas could be analyzed quantitatively. The analysis results are shown in Table 2.
  • the catalytic reaction apparatus used had 4
  • Reaction zones each with the catalyst layers and layer lengths defined in Table 1 in a salt bath cooled tubular reactor with 25 mm inner diameter.
  • the cesium content in the active composition shown in Table 1 generally drops except in the case of a catalytic apparatus containing only two
  • Catalyst devices having multiple catalyst layers (i.e., more than 2 layers) and the active mass content decreasing across all layers (ie, a decrease relative to the first compared to the last layer, regardless of whether there is still a variation between the first and last layers the active composition took place, ie, it could be arranged, for example, two layers of the same active material content between the first and last layer) showed the catalyst layers on from the first to the second sloping and then to the last layer an increasing activity profile.
  • the reaction tube was centrally arranged a 3 mm thermal sleeve with built-in tension element for temperature measurement. 4 Nm 3 of air with a loading of 30-100 g o-xylene / Nm 3 air (purity o-xylene> 99%) per hour through the tube from top to bottom at a total pressure of about 1450 mbar
  • the reaction zone was maintained at a salt bath temperature of 340 ° C, the second reaction zone was maintained at a salt bath temperature of 350 ° C, the third reaction zone was maintained at a salt bath temperature of 355 ° C, and the fourth reaction zone was maintained at a salt bath temperature of 360 ° C ,
  • the analysis of the reaction gas was carried out as in the comparative example. The analysis results are also given in Table 2.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
  • Catalysts (AREA)
  • Furan Compounds (AREA)

Abstract

L'invention concerne un procédé d'oxydation catalytique d'hydrocarbures en phase gazeuse qui comprend : a) la mise en place d'un réacteur de catalyse doté d'un espace réactionnel refroidi par un réfrigérant entre une arrivée de gaz et une sortie de gaz, et b) le passage d'un mélange réactionnel contenant un hydrocarbure dans l'espace réactionnel dans un sens d'écoulement du gaz. Selon ce procédé, le réfrigérant est mis à disposition avec un profil de température croissante dans le sens d'écoulement du gaz. L'invention concerne également un réacteur de catalyse correspondant.
EP11709121A 2010-03-19 2011-03-18 Procédé d'oxydation catalytique d'hydrocarbures en phase gazeuse et réacteur de catalyse Withdrawn EP2547670A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102010012090A DE102010012090A1 (de) 2010-03-19 2010-03-19 Verfahren zur katalytischen Gasphasenoxidation von Kohlenwasserstoffen und Katalysereaktionsvorrichtung
PCT/EP2011/054096 WO2011113920A1 (fr) 2010-03-19 2011-03-18 Procédé d'oxydation catalytique d'hydrocarbures en phase gazeuse et réacteur de catalyse

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EP2547670A1 true EP2547670A1 (fr) 2013-01-23

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DE102017210282A1 (de) * 2017-06-20 2018-12-20 Mahle International Gmbh Kolben für einen Verbrennungsmotor mit Flüssigmetallkühlung

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CN102869654A (zh) 2013-01-09
WO2011113920A1 (fr) 2011-09-22

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