WO2008135581A1 - Catalyseurs à base d'iridium destinés à la transformation d'hydrocarbures en présence de vapeur d'eau et notamment à la désalkylation à la vapeur d'hydrocarbures aromatiques à substitution d'alkyle - Google Patents

Catalyseurs à base d'iridium destinés à la transformation d'hydrocarbures en présence de vapeur d'eau et notamment à la désalkylation à la vapeur d'hydrocarbures aromatiques à substitution d'alkyle Download PDF

Info

Publication number
WO2008135581A1
WO2008135581A1 PCT/EP2008/055584 EP2008055584W WO2008135581A1 WO 2008135581 A1 WO2008135581 A1 WO 2008135581A1 EP 2008055584 W EP2008055584 W EP 2008055584W WO 2008135581 A1 WO2008135581 A1 WO 2008135581A1
Authority
WO
WIPO (PCT)
Prior art keywords
catalyst
weight
reaction
hydrocarbons
alkyl
Prior art date
Application number
PCT/EP2008/055584
Other languages
German (de)
English (en)
Inventor
Marco Bosch
Dirk Neumann
Götz-Peter SCHINDLER
Heinrich Laib
Armin Lange De Oliveira
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 WO2008135581A1 publication Critical patent/WO2008135581A1/fr

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
    • B01J23/54—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/56—Platinum group metals
    • B01J23/58—Platinum group metals with alkali- or alkaline earth metals
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
    • B01J23/54—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/56—Platinum group metals
    • B01J23/63—Platinum group metals with rare earths or actinides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/30—Catalysts, in general, characterised by their form or physical properties characterised by their physical properties
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
    • C01B3/40—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts characterised by the catalyst
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C4/00—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms
    • C07C4/08—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms by splitting-off an aliphatic or cycloaliphatic part from the molecule
    • C07C4/12—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms by splitting-off an aliphatic or cycloaliphatic part from the molecule from hydrocarbons containing a six-membered aromatic ring, e.g. propyltoluene to vinyltoluene
    • C07C4/14—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms by splitting-off an aliphatic or cycloaliphatic part from the molecule from hydrocarbons containing a six-membered aromatic ring, e.g. propyltoluene to vinyltoluene splitting taking place at an aromatic-aliphatic bond
    • C07C4/20—Hydrogen being formed in situ, e.g. from steam
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
    • B01J21/06—Silicon, titanium, zirconium or hafnium; Oxides or hydroxides thereof
    • B01J21/063—Titanium; Oxides or hydroxides thereof
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
    • B01J21/06—Silicon, titanium, zirconium or hafnium; Oxides or hydroxides thereof
    • B01J21/066—Zirconium or hafnium; Oxides or hydroxides thereof
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
    • B01J35/61—Surface area
    • B01J35/613—10-100 m2/g
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
    • B01J35/61—Surface area
    • B01J35/615—100-500 m2/g
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
    • B01J35/63—Pore volume
    • B01J35/633—Pore volume less than 0.5 ml/g
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
    • C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
    • C01B2203/0233—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a steam reforming step
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/10—Catalysts for performing the hydrogen forming reactions
    • C01B2203/1041—Composition of the catalyst
    • C01B2203/1047—Group VIII metal catalysts
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2521/00—Catalysts comprising the elements, oxides or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium or hafnium
    • C07C2521/06—Silicon, titanium, zirconium or hafnium; Oxides or hydroxides thereof
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
    • C07C2523/02—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of the alkali- or alkaline earth metals or beryllium
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
    • C07C2523/10—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of rare earths
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
    • C07C2523/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of noble metals
    • C07C2523/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of noble metals of the platinum group metals
    • C07C2523/46—Ruthenium, rhodium, osmium or iridium
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

Definitions

  • the present invention relates to an iridium-containing catalyst, its use for the reaction of hydrocarbons in the presence of water vapor and in particular its use for the dealkylation of alkyl-substituted aromatic hydrocarbons having 7 to 12 carbon atoms to benzene and a process for the reaction of hydrocarbons in the presence of Water vapor using the iridium-containing catalyst.
  • hydrocarbons in the presence of water vapor can be done by various reactions and processes.
  • a common process is the so-called steam reforming, in which the hydrocarbons are converted in the presence of water vapor to hydrogen, carbon monoxide and carbon dioxide.
  • Alkyl-substituted aromatic hydrocarbons can be reacted in the presence of steam in the so-called steam dealkylation to the corresponding aromatics, hydrogen, CO, CO 2 and further reaction products.
  • the dehydrogenation of hydrocarbons is often carried out in the presence of water, although the water does not participate in the actual dehydrogenation reaction. However, it has an advantageous effect on the catalyst service lives, since the water vapor reduces coke deposition by converting the coke into carbon monoxide and carbon dioxide.
  • US 4,233,186 describes a catalyst for the steam dealkylation of mono- and poly-alkyl-substituted aromatic hydrocarbons, the 0.1 to 5 wt .-% of a metal of group 8, 9 or 10 of the Periodic Table of the Elements (PSE, IUPAC nomenclature) on a Contains spinel carrier.
  • the carrier has the composition (M x MV x) Al 2 O 4, where M denotes a metal from group 8, 9 or 10 of the Periodic Table and M 'is a metal of Group 2, 7, 11 or 12 of the PTE.
  • No. 4,207,169 discloses a catalytic process for the steam dealkylation of alkyl-substituted aromatics on catalysts based on an alumina carrier which contains 0.1 to 1% by weight of rhodium and 0.05 to 1% by weight of titanium dioxide. On the catalyst support further metals of the Pt group, alkali metals and other metals may be applied.
  • No. 3,775,504 relates to the dealkylation of alkyl-substituted aromatics in the presence of water vapor over catalysts comprising at least one group 8, 9 or 10 metal of the PSE on a support, the support comprising at least 50% by weight of ⁇ -Al 2 O 3 has.
  • the catalyst may optionally contain alkali and alkaline earth oxides.
  • the reaction of the alkyl-substituted aromatics proceeds not only in accordance with the steam dealkylation reaction but also with consumption of the resulting hydrogen according to the hydrodealkylation reaction in which alkyl-substituted aromatics react to the corresponding aromatics and alkanes. Both reactions are catalyzed by the same catalyst.
  • Alumina-based catalysts each containing a Group 8, 9 or 10 metal of the PSE, are compared by rhodium-based relative "turn over frequencies" (TOF), which provides a measure of the catalytic activity of the individual metals Rhodium is the most active metal by far and iridium is one of the least active metals, by definition the relative TOF of rhodium is 100%, but iridium is 14% or less Selectivities of the various platinum metals in the vapor dealkylation of toluene to benzene, the metals Rh, Pd, Os, Ir, and Pt have higher benzene selectivities than Ni, Co, and Ru.
  • TOF turn over frequencies
  • Rh perform significantly better than Rh Pt,
  • Pd and Ir have higher selectivities to benzene in the vapor dealkylation of toluene, but at the same time they are significantly less reactive than Rh.
  • Rh is that in catalyzato For the vapor dealkylation of alkyl-substituted aromatics the most commonly used metal. This leads to a dependence on this metal, which can have a negative economic impact on fluctuating raw material costs.
  • the object of the present invention is therefore to provide an alternative catalyst for the reaction of hydrocarbons in the presence of water vapor, with which similar or better yields can be achieved as with the catalysts of the prior art.
  • the catalyst should have long-term stability and high yields even at low molar S / C ratios (steam to carbon, molar ratio of water vapor molecules to C atoms present in the mixture), since less is present at low S / C ratios Steam to be heated and condensed in the workup of the reaction mixture again. This has the consequence that the heat exchanger surfaces can be made smaller.
  • the erf ⁇ ndungswashe catalyst contains as component a) 0.1 to 3 wt .-%, based on the total weight of the catalyst, iridium. In a preferred embodiment, the catalyst contains from 0.2 to 2.0% by weight, preferably from 0.4 to 1.6% by weight, based on the total weight of the catalyst, of iridium.
  • the catalyst according to the invention contains 0.1 to 10.0% by weight, based on the total weight, of at least one promoter, preferably 0.5 to 8.0% by weight, particularly preferably 1.5 to 5, 0th
  • the promoter is selected from the group comprising alkali metals, alkaline earth metals and lanthanides. Particularly preferred promoters are Cs, Ba, Sr, La, Ce, Pr, Nd and Eu.
  • the promoter (s) may be applied to the carrier in the form of their salts, as described below. However, after calcination and activation of the catalyst, they are preferably present as oxides in the catalyst.
  • the catalyst contains a promoter from the above-mentioned group.
  • two promoters from the above-mentioned group are used.
  • the catalyst according to the invention comprises, as component c), 87.0 to 99.8% by weight, based on the total weight of the catalyst, of a support which contains zirconium oxide (ZrO 2).
  • the zirconium oxide may optionally contain 0 to 20% by weight, based on the weight of the zirconium oxide, of one or more elements selected from the group Si, Y, Ce and La as stabilizer.
  • the ZrO 2 may be in monoclinic or tetragonal crystal structure or in mixed crystal structure (X. Turrillas, J. Mater. Res. 1993, 8, 163-168).
  • the stabilizer or stabilizers serve to stabilize a specific crystal structure of the zirconium oxide (R. Franklin et al., Catal. Today 1991, 10, 405-407).
  • the crystal structure of the zirconia can be determined by taking an XRD spectrum. This is a common method of X-ray diffraction.
  • the stabilized zirconium oxide-containing support preferably contains cerium, lanthanum, yttrium and / or silicon, in particular cerium (III) oxide, lanthanum (III) oxide and / or silicon (IV) oxide.
  • cerium (III) oxide, lanthanum (III) oxide and / or silicon (IV) oxide can be used.
  • the stabilized zirconium oxide-containing carrier usually contains up to 15% by weight, preferably 1 to 10% by weight, in particular 3 to 7% by weight, based on the weight of Zirconium oxide, cerium (III) oxide.
  • the stabilized zirconia-containing support usually contains up to 15% by weight, preferably from 2 to 15% by weight, in particular from 5 to 15% by weight, based on the weight of zirconium oxide , Lanthanum (III) oxide
  • the stabilized zirconium oxide-containing support usually contains up to 10% by weight, preferably 1 to 7% by weight, in particular 2 to 5% by weight, based on the Weight of zirconium oxide, silicon (IV) oxide.
  • the stabilized zirconium oxide-containing support generally contains up to 20% by weight, preferably 5 to 15% by weight, in particular 10 to 15 wt .-%, based on the weight of zirconium oxide, cerium (III) oxide and usually up to 20 wt .-%, preferably 1 to 15 wt .-%, in particular 2 to 10 wt. -%, based on the weight of zirconium oxide, lanthanum (III) oxide.
  • the support preferably contains oxides from the group of zirconium oxide having a tetragonal crystal structure, zirconium oxide having a monoclinic crystal structure and stabilized zirconium oxide having a tetragonal crystal structure. Particularly preferred is stabilized zirconia having a tetragonal crystal structure.
  • the amount specified for component c) from 87.0 to 99.8 wt .-% applies to the non-stabilized oxide or oxide mixture as well as for the one or more stabilizers containing oxide or oxide mixture, based on the total amount of the catalyst.
  • the carrier c) may also contain auxiliaries. These are suitable for facilitating the shaping of the carrier. Usual aids are, for example, graphite and waxes, but it is also possible to use silicon dioxide and aluminum oxide as auxiliaries. Another common tool is pore former. These adjuvants can either be added by themselves or in the form of their precursors that are convert to the appropriate excipient during calcining. Examples include silicon dioxide precursors such as tetraethyl orthosilicate (TEOS) and colloidal silica and alumina precursors such as Boehmite, for example Pural ® (Fa. Sasol). Preferably, aluminas are used as auxiliaries.
  • TEOS tetraethyl orthosilicate
  • alumina precursors such as Boehmite
  • aluminas are used as auxiliaries.
  • the carrier c) may contain up to 10% by weight, based on the total weight of the carrier, of auxiliaries.
  • the carrier contains from 0.1 to 10% by weight, preferably from 0.5 to 2% by weight, based on the total weight of the carrier, of auxiliaries.
  • the preparation of the catalyst can be carried out by customary methods known to the person skilled in the art.
  • the zirconia-containing support from corresponding compounds which convert to the corresponding oxide upon calcining.
  • hydroxides, carbonates and carboxylates are suitable.
  • the corresponding oxide or precursors, which are converted to the oxide upon calcination may be prepared by methods known per se, e.g. according to the So 1 gel method, by precipitation, dewatering of the corresponding carboxy late, dry mixing, slurrying or spray drying. In the precipitation, usually soluble metal salts are used, e.g. the corresponding halides, preferably chloride, alkoxides, nitrate, etc., preferably nitrate.
  • Stabilized zirconia-containing supports can i.a. can be prepared by zirconium oxide or the corresponding precursor with soluble salts of the stabilizers, such as described above.
  • the corresponding halides preferably chlorides, alkoxides, nitrates, etc., soaks.
  • the stabilizers on the zirconia-containing carrier by precipitation from corresponding soluble salts of the stabilizers.
  • the corresponding halides preferably chlorides, alkoxides, nitrates, etc., are generally suitable.
  • the stabilized zirconium oxide-containing support from compounds which on calcining convert into zirconium oxide or cerium (III) oxide, lanthanum (III) oxide, silicon (IV) oxide.
  • hydroxides, carbonates and carboxylates are suitable. These are for example precipitated together, spray-dried together etc.
  • the zirconia and stabilized zirconia or precursors prepared by the above processes may be added with the above-mentioned auxiliary agents suitable for facilitating the shaping of the zirconia-containing carrier. Subsequently, the shaping takes place.
  • strands, tablets, spheres, chippings, monoliths, etc. are prepared by the usual methods.
  • the zirconium oxide described above and the stabilized zirconium oxides or the corresponding precursors, which are optionally mixed with auxiliaries, are calcined. This is usually done with air or a mixture of air and nitrogen, at a temperature of 300 to 800 0 C, preferably at 500 to 600 0 C. It may be advantageous to add water vapor to the air or the air / nitrogen mixture.
  • the iridium can now be applied to the zirconia-containing support.
  • the carrier is impregnated with a solution of an iridium precursor.
  • the impregnation can be carried out by the incipient-wetness method, in which the porous volume of the support is filled up with approximately the same volume of impregnating solution and, optionally after maturation, the support is dried; or you work with an excess of solution, the volume of this solution is greater than the porous volume of the carrier.
  • the carrier is mixed with the impregnating solution and stirred for a sufficient time. Furthermore, it is possible to spray the carrier with a solution of the metal precursor.
  • Suitable iridium precursors are the respective metal salts, i.a. Halides, especially chloride, nitrate, acetate, alkaline carbonates, formate, oxalate, citrate, tartrate, iridium-organic compounds, but also iridium complexes.
  • the latter may contain as ligands acetylacetonate, amino alcohols, carboxylates such as oxalates, citrates, etc. or hydroxycarboxylic acid salts, etc.
  • Promoted catalysts are prepared by applying the promoter precursor or the promoter precursors in analogy to the methods for iridium application.
  • Suitable promoter precursors include halides, especially chlorides, nitrates, acetates, alkaline carbonates, formates, oxalates, citrates, tartrates, corresponding me- organometallic compounds, but also promoter complexes.
  • the latter may contain as ligands acetylacetonate, amino alcohols, carboxylates such as oxalates, citrates, etc. or hydroxycarboxylic acid salts, etc.
  • the promoter precursor can be applied together with the iridium precursors. But it is also possible to apply them one after the other. It may also be advantageous to apply the individual precursors in a certain order.
  • the promoter precursors can be applied together or separately. It is also possible to apply the iridium precursor together or separately with one or more promoter precursors. In the case of a separate application, it may also be advantageous to apply the individual precursors in a certain order. Between the applications of the individual solutions, the impregnated carrier can be dried before the next solution is applied.
  • the zirconia-containing support on which the iridium precursor and the promoter precursor (s) has been applied is calcined.
  • the calcination is usually carried out with air or a mixture of air and nitrogen, at a temperature of 300 to 800 0 C, preferably at 400 to 600 0 C. It may be advantageous to add water vapor to the air or the air / nitrogen mixture ,
  • the catalyst thus obtained is usually activated before its use, the reaction of hydrocarbons in the presence of water vapor. For this he is with
  • the activation process is in
  • Presence of water vapor performed.
  • the activation of the catalyst is usually carried out in the reactor in which the reaction of the hydrocarbons is to take place. However, it is also possible to carry out the activation of the catalyst before installation in the corresponding reactor.
  • the catalyst usually has a BET surface area (determined to DIN 66131) of up to 500 m 2 / g, preferably from 10 to 300 m 2 / g, in particular from 20 to 200 m 2 / g, particularly preferably at least 25 m 2 / g on.
  • the pore volume of the catalyst is 0.1 to 1 ml / g, preferably 0.15 to 0.8 ml / g, in particular 0.2 to 0.6 ml / g.
  • the support preferably has a monomodal or bimodal pore size distribution, the proportion of pores having a diameter greater than 10 nm being at least 30% by volume.
  • the cutting hardness of the carrier is at least 5 N / mm.
  • the cutting hardness was measured on a Zwick type BZ2.5 / TS1S apparatus with a preliminary force of 0.5 N, a precursor thrust speed of 10 mm / min, and a subsequent test speed of 1.6 mm / min, certainly.
  • the device had a fixed turntable and a freely movable punch with built-in cutting edge of 0.3 mm thickness.
  • the movable punch with the cutting edge was connected to a load cell for power absorption and moved during the measurement against the fixed turntable on which the catalyst molding to be examined was located.
  • the tester was controlled by a computer, which registered and evaluated the measurement results. The values obtained represent the average of the measurements for each of 10 shaped catalyst bodies.
  • the shaped catalyst bodies had a cylindrical geometry with their average length approximately equal to two to three times the diameter, and were measured with the blade of 0.3 mm thickness loaded with increasing force until the molding was severed.
  • the cutting edge was applied perpendicular to the longitudinal axis of the molding on the molding.
  • the required force per mm diameter of the carrier is the cutting hardness (unit N / mm).
  • catalysts are used in which the dispersity of iridium is at least 20%. The dispersity is measured by volumetric measurement of CO uptake 40 0 C after reduction of the metal atoms in the presence of hydrogen at 450 0 C for at least 2h.
  • the iridium When applied to the substrate, the iridium has a radial concentration distribution on the substrate, with the major portion, i. at least 55% of the iridium, or located directly below the surface of the support material. Such catalysts are also referred to as shell catalysts.
  • the layer in which the iridium is on the substrate usually has a thickness of 50 to 350 micrometers.
  • Another object of the present invention is the use of the above-described catalyst for the reaction of hydrocarbons in the presence of water vapor.
  • These reactions include, for example, steam reforming, in which hydrocarbons are catalytically converted to hydrogen, carbon monoxide, and carbon dioxide in the presence of water vapor, and steam dealkylation, in which alkyl-substituted aromatic hydrocarbons react to aromatics, hydrogen, carbon monoxide, and carbon dioxide.
  • the dehydrogenation of hydrocarbons in the presence of water is counted among these reactions, although the water vapor is not involved in the actual dehydrogenation reaction, but its presence has a positive effect on the life of the catalyst.
  • the water vapor reduces the deposition of coke and can react with the coke to form hydrogen and carbon monoxide or carbon dioxide.
  • the catalyst according to the invention is preferably used for reacting hydrocarbons having 1 to 12 carbon atoms in the presence of steam. Particular preference is given to reacting mixtures of hydrocarbons having 5 to 10 carbon atoms which are formed in the streamcracker as a by-product in the production of ethylene and / or propylene from naphtha.
  • this is the so-called pyrolysis gasoline, which is obtained after hydrotreating (removal of sulfur components, dienes and olefins with the aid of hydrogen).
  • the pyrolysis gasoline typically consists of a mixture of saturated linear and branched hydrocarbons (paraffins), saturated cyclic hydrocarbons (naphthenes) and alkyl-substituted aromatics.
  • the ratio of saturated hydrocarbons to alkyl-substituted aromatics is typically between 5:95 and 95:75.
  • Individual fractions, such as hydrocarbons with 5 carbon atoms (Cs cut) can be obtained by distillative separation.
  • the separation of the paraffin and naphthenic mixtures of the alkyl-substituted aromatics succeed, for example, by an extractive distillation.
  • the use of the above-described catalyst for the steam dealkylation of alkyl-substituted aromatic hydrocarbons is preferred.
  • Another object of the present invention is a process for the reaction of hydrocarbons in the presence of steam on the catalyst of the invention described above, preferably the reaction of Kohlenwasserstof fen with 1 to 12 carbon atoms.
  • Another preferred object of the present invention is a process for the preparation of benzene by reacting alkyl-substituted benzenes having 7 to 12 carbon atoms in the presence of water vapor on the catalyst according to the invention described above.
  • alkyl-substituted aromatic hydrocarbons can be dealkylated in the presence of the catalyst described above.
  • Alkyl in the context of the present invention means branched and linear C 1 -C 6 -alkyl groups.
  • One or more alkyl-substituted aromatic hydrocarbons means that one, two or more of the H atoms attached to the aromatic nucleus can be replaced by alkyl up to the case where all the corresponding H atoms have been replaced by alkyl.
  • aromatics and “aromatic hydrocarbons” are used synonymously.
  • one or more alkyl-substituted benzenes containing 7 to 12 carbon atoms may be dealkylated.
  • suitable mono-alkyl-substituted benzenes such as toluene, ethylbenzene or propylbenzene, polyhydric alkyl-substituted benzenes such as o-, m- and p-xylenes, mesitylene and mixtures thereof.
  • toluene is used.
  • mixtures containing substantially mono- and poly-alkyl-substituted benzenes are used; For example, the resulting during steam cracking so-called TX cut.
  • Sources of the mono- and poly-alkyl-substituted benzenes having 7 to 12 carbon atoms to be used according to the present invention are:
  • Cokererase extract obtained by scrubbing gas with higher boiling hydrocarbons and / or by adsorption on activated charcoal from raw coal resulting from the coking of coal
  • coal extract obtained by extraction of coal and / or brown coal with solvent such as tetralin or toluene at 350-400 0 C and 100-300 bar,
  • Aromatic fraction which is formed during the reaction of synthesis gas with methanol on zeolite catalysts or directly from synthesis gas by reaction on a bifunctional catalyst such as ZSM-5 / zinc chromite,
  • the feed stream used in the steam dealkylation generally contains at least 50% by weight, preferably at least 80% by weight, particularly preferably at least 90% by weight, of a mono- or polysubstituted alkyl-substituted aromatic hydrocarbon or a mixture thereof ,
  • a feed stream which, in addition to the mono- or poly-alkyl-substituted aromatic hydrocarbon or mixtures thereof, up to 50 wt .-%, preferably up to 30 wt .-%, particularly preferably to to 20 wt .-% of non-aromatics having 7 to 12 carbon atoms.
  • non-aromatics may be paraffins and / or naphthenes.
  • the feed stream may contain up to 40% by weight, preferably up to 10% by weight, more preferably up to 2% by weight, of hydrocarbons having 5 and / or 6 carbon atoms.
  • the so-called BTX cut which is obtained in steam cracking, can also be used as the feed stream.
  • the feed stream may contain sulfur containing compounds, such as e.g. Mercaptans, thiophene, benzothiophene, alkyl-substituted thiophenes and / or benzothiophenes.
  • sulfur containing compounds such as e.g. Mercaptans, thiophene, benzothiophene, alkyl-substituted thiophenes and / or benzothiophenes.
  • the sulfur content of the feed stream may be up to 100 ppm, usually 10 ppm or less, more preferably 2 ppm or less.
  • the dealkylation is usually carried out from 300 to 800 ° C., preferably from 400 to 600 ° C., in particular from 400 to 550 ° C.
  • the pressure is in this case in a range of 1 to 50 bar, preferably from 3 to 30 bar, in particular from 5 to 25 bar.
  • the LHSV Liquid Hourly Space Velocity
  • the LHSV is usually 0.1 to 10 parts by volume of feed stream per part by volume of catalyst per hour (l / l * h), preferably 0.5 to 5 1/1 h, especially at 1 to 3 (l / l «h).
  • the molar ratio of steam / carbon is generally from 0.1 to 10, preferably from 0.2 to 5, in particular from 0.5 to 2.
  • the feed used and the water is evaporated in an evaporator at 100 to 400 0 C, this steam brought in a preheater and / or by a heat network to the desired reaction temperature, preferably at 400 to 600 0 C, in particular 400 to 550 0 C and then introduced into the reactor.
  • Coke and / or coke precursors can form at the active centers and in the pores of the catalyst.
  • Coke is usually high-boiling unsaturated hydrocarbons.
  • Coke precursors are typically low-boiling alkenes, alkynes and / or saturated high molecular weight hydrocarbons.
  • the deposition of the coke or coke precursor has the effect that the activity and / or selectivity of the catalyst is adversely affected.
  • the aim of the regeneration is the removal of the coke or the coke precursor, without the physical properties of the catalyst being adversely affected.
  • the coke precursors can be removed in the presence of an oxygen-containing gas mixture by evaporation in the presence of an inert gas at an elevated temperature (T> 250 0 C) and / or hydrogenation in the presence of a wasserstoffhal- term gas mixture and / or incineration.
  • the regeneration of the catalyst can be carried out in situ or ex situ, preferably an in situ regeneration is carried out.
  • the inlet temperature for the oxidative regeneration is usually between 350 and 550 ° C.
  • the oxygen concentration of the oxygen-containing gas mixture is usually between 0.1 and 10% by volume.
  • the pressure is typically between 0.1 and 10 bar.
  • the oxidative regeneration of the catalyst is carried out in the presence of water vapor.
  • the reactors used are generally fixed-bed reactors, tube-bundle reactors or fluid-bed reactors.
  • the reaction of the alkyl-substituted aromatics by means of steam dealkylation is an endothermic reaction.
  • the heat required to maintain the reaction can be supplied by heating from the outside. In this case, the reaction or reaction zones can be heated, but it is also possible to switch between two reactors or reaction zone an intermediate heating and to heat the reaction mixture.
  • the reaction can also be carried out autothermally, i. the heat requirement of the conversion is covered by a second, exothermic reaction in the system itself.
  • the desired reaction temperature may be established by feeding an oxygen-containing gas into the catalyst bed and by combustion of a portion of the feed hydrocarbon and / or a portion of the dealkylation catalyst The resulting hydrogen and / or the carbon monoxide forming during the reaction and / or the coke formed in the reaction, which generates the necessary heat, whereupon the oxidation is assisted by the catalyst used as an oxygen.
  • enriched air such as a mixture of oxygen and nitrogen, or pure oxygen, but other oxygenated gases may be used in addition to enriched air, provided that the other components of the mixture are inert under the reaction conditions.
  • the supply of the oxygen-containing gas can take place at one or more points of the reactor used / the reactors used, in particular at one or more points along the catalyst bed (s). It is also possible to add the oxygen-containing gas already to the hydrocarbon feed used and the water vapor.
  • the process can be designed so that the dealkylation reaction and the oxidation reaction are carried out in different regions.
  • This is possible in particular in a tray reactor, but also in a cascade of fixed bed reactors.
  • the reaction zones of the vapor decomposition and the reaction zones of the oxidation preferably alternate.
  • respective combustion chambers are interposed between the reactors in which the oxygen-containing gas is reacted with a portion of the hydrocarbon feed and / or a portion of the hydrogen formed in the steam dealkylation, the latter being preferred.
  • the reaction of the hydrogen formed in the reaction with the oxygen of the oxygen-containing gas can be carried out in the presence or in the absence of oxidation catalysts.
  • the oxidation catalysts used are those known to those skilled in the art, preference being given to those which are selective with respect to the oxidation of hydrogen with oxygen, in order to avoid undesired consumption of hydrocarbons used by oxidation.
  • the oxidation catalysts contain, as described in US 4,435,607, a noble metal of groups 8, 9 or 10 of the Periodic Table on a porous support.
  • metals of group 4 can be contained, and if desired, at least one metal of groups 1 or 2 of the periodic table.
  • alumina carriers are preferably used as the carrier.
  • the reaction is carried out in the presence of an oxidation catalyst, in particular if the steam dealkylation reaction and the oxidation reaction are carried out in different regions, for example in a tray reactor or in a reactor cascade with interposed combustion chambers.
  • the molar ratio of oxygen / carbon is usually so It is established that the oxidation of the hydrogen formed in the dealkylation reaction and, if appropriate, the carbon monoxide formed in the steam dealkylation reaction and, if appropriate, the coke formed during the reaction, can produce the heat necessary to maintain the reaction temperature. Furthermore, the molar ratio of oxygen / carbon is adjusted so that practically no hydrocarbons used or formed are burned with the oxygen. In general, the molar ratio of oxygen / carbon is from 1:10 to 1: 2000, preferably from 1:50 to 1: 1000, in particular from 1: 100 to 1: 900.
  • the reaction gas obtained by the process according to the invention is rich in hydrogen and dealkylated aromatic hydrocarbons, in particular benzene and / or alkyl-substituted aromatic hydrocarbons, whose number of alkyl radicals is reduced compared to the alkyl-substituted aromatic hydrocarbons used.
  • the reaction gas contains benzene as the aromatic hydrocarbon, especially for the case when the alkyl-substituted aromatic hydrocarbon used is mainly toluene.
  • Paraffinic compounds may possibly be partially decomposed to methane, carbon dioxide and hydrogen.
  • the dealkylated aromatic hydrocarbons formed and the arm gas formed, which contains the hydrogen formed in the reaction according to the invention, are separated from the reaction gas by customary processes. Furthermore, the arm gas or the hydrogen separated therefrom can be returned to the reaction apparatus.
  • the ratio between cycle gas (in Nl) and feed (in kg) is from 10: 1 to 2000: 1, preferably from 20: 1 to 1000: 1 and especially from 50: 1 to 500: 1.
  • the feed used and the water are evaporated in an evaporator at 100 to 400 0 C, this vapor in a preheater to the desired reaction temperature brought, which is preferably at 400 to 600 0 C, in particular at 400 to 550 0 C, and then introduced into the reactor.
  • the oxygen-containing gas preferably air, is fed.
  • the reaction gas which is obtained according to the erf ⁇ ndungsdorfen method, is passed from the reactor into a heat exchanger and cooled there, preferably at 10 to 100 0 C. It is expedient to integrate the heat released in this process in the process (heat combination), for example to heat the feed stream or other streams to be heated (eg evaporator of the column).
  • the forming liquid phase containing the dealkylated aromatic hydrocarbon, preferably benzene is fed to a phase separator and the organic phase is separated from the water phase. If desired, the organic phase containing the dealkylated aromatic hydrocarbon, preferably benzene, can be further purified, for example by distillation. If desired, the separated off-gas may be returned to the reactor.
  • benzene and, if appropriate, impurities are removed via overheads and hydrocarbons having 7 or more carbon atoms are removed via the bottom in a distillation column.
  • the separated mixture can be recycled to the steam dealkylation.
  • the benzene fraction can be passed to a further distillation column in which the dissolved water and the low boilers are passed overhead via azeotropic distillation Reinbenzol be separated via sump.
  • the columns are carried out as columns with side draw or as dividing wall columns.
  • This embodiment of the process according to the invention makes it possible to produce benzene in high purity, the hydrogen which is formed in the steam dealkylation reaction being used, via a coupling with an oxidation reaction, the heat required, the reaction temperature uphold, win. Therefore, on the one hand, the hydrogen formed can be used immediately, and further the heat is formed directly in the reactor, so that heat losses e.g. can be avoided on external heat exchangers.
  • the monoclinic zirconia support and the Si-stabilized tetragonal zirconia support are commercially available from NorPro under designation SZ 3164 and SZ 6152, respectively.
  • the La, Ce-stabilized tetragonal zirconia support and Ce-stabilized zirconia support were obtained by deformation of the corresponding zirconium hydroxide precursors respectively at the company.
  • the titanium oxide support is the commercially available product P25 from Degussa.
  • BET BET surface area
  • PV pore volume
  • the catalysts were prepared by impregnation of the support material to the maximum water absorption (incipient wetness method). For this purpose, water-soluble salts of the components to be applied were combined together in a solution and the carrier material was impregnated with this solution. In the subsequent step, the catalysts were dried for at least 6 h at 80 0 C. Optionally, the impregnation was repeated to obtain the desired concentrations of the elements on the support. After drying, the catalysts were calcined in a muffle furnace with air addition for 3 hours at 500 0 C.
  • the composition was redetermined after a total run time of 24 hours. Subsequently, reaction was further 12 h at 500 0 C, however, at a LHSV of 1 h "continued 1 (setting III), and again determines the composition of the product stream after 36 hours total run time.
  • composition The analysis of the composition is carried out by gas chromatography.
  • the results are shown in the following Tables 2 to 6.
  • the conversion refers to the conversion of toluene, the selectivity is the benzene selectivity in mol%.
  • the conversion and selectivity were calculated from the gas chromatographic data.
  • the percentages in the parentheses behind the elements indicate the concentration of each element in weight percent based on the total weight of the catalyst.
  • the elements listed under composition are the iridium and the elements of component b) used as promoters.
  • the column Carrier lists the zirconium oxide or stabilized zirconium oxide used as support, which is contained in the catalyst as component c).

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Inorganic Chemistry (AREA)
  • Catalysts (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

L'invention concerne un catalyseur contenant de l'iridium, son utilisation pour la transformation d'hydrocarbures en présence de vapeur d'eau et notamment son utilisation pour la désalkylation à la vapeur d'hydrocarbures aromatiques à substitution d'alkyle comportant 7 à 12 atomes de carbone pour obtenir du benzol. L'invention porte également sur un procédé de transformation d'hydrocarbures en présence de vapeur d'eau au moyen de ce catalyseur contenant de l'iridium.
PCT/EP2008/055584 2007-05-08 2008-05-07 Catalyseurs à base d'iridium destinés à la transformation d'hydrocarbures en présence de vapeur d'eau et notamment à la désalkylation à la vapeur d'hydrocarbures aromatiques à substitution d'alkyle WO2008135581A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
EP07107737.4 2007-05-08
EP07107737 2007-05-08

Publications (1)

Publication Number Publication Date
WO2008135581A1 true WO2008135581A1 (fr) 2008-11-13

Family

ID=39730711

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP2008/055584 WO2008135581A1 (fr) 2007-05-08 2008-05-07 Catalyseurs à base d'iridium destinés à la transformation d'hydrocarbures en présence de vapeur d'eau et notamment à la désalkylation à la vapeur d'hydrocarbures aromatiques à substitution d'alkyle

Country Status (1)

Country Link
WO (1) WO2008135581A1 (fr)

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2011138356A1 (fr) 2010-05-07 2011-11-10 Basf Se Procédé de production de gaz de synthèse et d'au moins une matière valorisable organique liquide ou liquéfiable
WO2011138355A2 (fr) 2010-05-07 2011-11-10 Basf Se Procédé de production de cellulose et d'au moins une matière valorisable organique liquide ou liquéfiable avec recyclage des effluents gazeux
WO2011138357A1 (fr) 2010-05-07 2011-11-10 Basf Se Procédé de préparation d'au moins une matière valorisable aromatique de faible poids moléculaire à partir d'une matière de départ contenant de la lignine
WO2012013735A1 (fr) 2010-07-29 2012-02-02 Basf Se Composition contenant un catalyseur et de la lignine, et utilisation de ladite composition pour la production d'une composition aromatique
WO2012160072A1 (fr) 2011-05-24 2012-11-29 Basf Se Procédé de production de polyisocyanates à partir de biomasse
WO2014001423A1 (fr) * 2012-06-29 2014-01-03 Basf Se Procédé haute pression permettant de soumettre des hydrocarbure à un reformage au dioxyde de carbone réalisé en présence de matière actives contenant de l'iridium
US8933262B2 (en) 2011-05-24 2015-01-13 Basf Se Process for preparing polyisocyanates from biomass

Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1505112A (en) * 1974-03-01 1978-03-22 Inst Francais Du Petrole Catalytic hydrodealkylation of alkylaromatic hydrocarbons
US4233186A (en) * 1978-03-20 1980-11-11 Elf Union Catalysts for water dealkylation of aromatic hydrocarbons
FR2464095A1 (fr) * 1979-08-27 1981-03-06 Catalyse Soc Prod Francais Nouveaux catalyseurs de conversion d'hydrocarbures
JPS5691843A (en) * 1979-12-26 1981-07-25 Babcock Hitachi Kk Catalyst for steam-dealkylation reaction of alkylbenzene
US4297205A (en) * 1978-09-28 1981-10-27 Standard Oil Company (Indiana) Reforming with a catalyst comprising iridium, zirconia, and alumina
US20020037938A1 (en) * 1999-06-25 2002-03-28 Hongyuan Luo Process and catalyst for preparing C2-oxygenates from synthesis gas
EP1356863A1 (fr) * 2000-11-17 2003-10-29 Osaka Gas Company Limited Catalyseur utile pour purifier des gaz residuaires contenant du methane et procede de purification de gaz residuaires contenant du methane
EP1712278A1 (fr) * 2004-12-20 2006-10-18 Tanaka Kikinzoku Kogyo Kabushiki Kaisha Catalyseur de combustion pour le traitement de gaz d'echappement diesel et procede de traitement de gaz d'echapement diesel

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1505112A (en) * 1974-03-01 1978-03-22 Inst Francais Du Petrole Catalytic hydrodealkylation of alkylaromatic hydrocarbons
US4233186A (en) * 1978-03-20 1980-11-11 Elf Union Catalysts for water dealkylation of aromatic hydrocarbons
US4297205A (en) * 1978-09-28 1981-10-27 Standard Oil Company (Indiana) Reforming with a catalyst comprising iridium, zirconia, and alumina
FR2464095A1 (fr) * 1979-08-27 1981-03-06 Catalyse Soc Prod Francais Nouveaux catalyseurs de conversion d'hydrocarbures
JPS5691843A (en) * 1979-12-26 1981-07-25 Babcock Hitachi Kk Catalyst for steam-dealkylation reaction of alkylbenzene
US20020037938A1 (en) * 1999-06-25 2002-03-28 Hongyuan Luo Process and catalyst for preparing C2-oxygenates from synthesis gas
EP1356863A1 (fr) * 2000-11-17 2003-10-29 Osaka Gas Company Limited Catalyseur utile pour purifier des gaz residuaires contenant du methane et procede de purification de gaz residuaires contenant du methane
EP1712278A1 (fr) * 2004-12-20 2006-10-18 Tanaka Kikinzoku Kogyo Kabushiki Kaisha Catalyseur de combustion pour le traitement de gaz d'echappement diesel et procede de traitement de gaz d'echapement diesel

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2011138356A1 (fr) 2010-05-07 2011-11-10 Basf Se Procédé de production de gaz de synthèse et d'au moins une matière valorisable organique liquide ou liquéfiable
WO2011138355A2 (fr) 2010-05-07 2011-11-10 Basf Se Procédé de production de cellulose et d'au moins une matière valorisable organique liquide ou liquéfiable avec recyclage des effluents gazeux
WO2011138357A1 (fr) 2010-05-07 2011-11-10 Basf Se Procédé de préparation d'au moins une matière valorisable aromatique de faible poids moléculaire à partir d'une matière de départ contenant de la lignine
WO2012013735A1 (fr) 2010-07-29 2012-02-02 Basf Se Composition contenant un catalyseur et de la lignine, et utilisation de ladite composition pour la production d'une composition aromatique
WO2012160072A1 (fr) 2011-05-24 2012-11-29 Basf Se Procédé de production de polyisocyanates à partir de biomasse
US8933262B2 (en) 2011-05-24 2015-01-13 Basf Se Process for preparing polyisocyanates from biomass
WO2014001423A1 (fr) * 2012-06-29 2014-01-03 Basf Se Procédé haute pression permettant de soumettre des hydrocarbure à un reformage au dioxyde de carbone réalisé en présence de matière actives contenant de l'iridium

Similar Documents

Publication Publication Date Title
EP0948475B1 (fr) Procede de production d'olefines, en particulier de propylene, par deshydrogenation
EP1322578B1 (fr) Procede pour deshydrogener des hydrocarbures
EP0714872B1 (fr) Catalyseur pour la déshydrogénation de paraffines C6-C15
DE2839795C2 (de) Platingruppenmetall enthaltender Katalysator und dessen Verwendung
DE60306973T2 (de) Verfahren zur katalytischen Dehydrierung von Kohlenwasserstoffen unter Verwendung von Kohlendioxid als weiches Oxidationsmittel
EP1074301B1 (fr) Catalyseur avec une répartition bimodale de la taille des pores
WO2008135581A1 (fr) Catalyseurs à base d'iridium destinés à la transformation d'hydrocarbures en présence de vapeur d'eau et notamment à la désalkylation à la vapeur d'hydrocarbures aromatiques à substitution d'alkyle
DE10060099A1 (de) Regenerierung eines Dehydrierkatalysators
DE2030337A1 (fr)
WO2008148807A1 (fr) Procédé amélioré de transformation d'hydrocarbures sur un catalyseur en présence de vapeur d'eau
WO2008135582A1 (fr) Catalyseurs à base d'iridium et de palladium destinés à la transformation d'hydrocarbures en présence de vapeur d'eau et notamment à la désalkylation à la vapeur d'hydrocarbures aromatiques à substitution d'alkyle
DE60035449T2 (de) Katalysator mit guter Ereichbarkeit und mit Elementen der Grupen 8, 9 und 10, und seine Verwendung in einem Verfahren für die Dehydrierung von Paraffinen
WO2007051851A1 (fr) Procede de production de composes aromatiques, en particulier de benzene, par aromatisation de composes non aromatiques a la vapeur d'eau et desalkylation d'hydrocarbures aromatiques a substitution alkyle a l'hydrogene
DE69817282T2 (de) Neue Katalysatoren für die Umwandlungsreaktionen von organischen Verbindungen
WO2007051855A2 (fr) Procede de production de benzene et de composes alkyl-aromatiques par desalkylation autothermique a la vapeur d'eau
WO2007051852A2 (fr) Procede de desalkylation d'hydrocarbures aromatiques a substitution alkyle a la vapeur d'eau
EP1966111B1 (fr) Procede de transformation d un hydrocarbure aromatique en presence d hydrogene
WO2007051856A1 (fr) Procede d'aromatisation de composes non aromatiques et de desalkylation d'hydrocarbures aromatiques a substitution alkyle a la vapeur d'eau
DE2037927A1 (de) Verfahren zur Reformierung von naphthen und paraffinhaltigen Erdolkohlenw asserstoffen
DE2910938A1 (de) Reduziertes, katalytisches, zusammengesetztes produkt
EP1351765B1 (fr) Catalyseur a repartition bimodale du rayon des pores
WO1997040931A1 (fr) Catalyseur pour aromatisation selective
DE2030364C3 (de) Verfahren zum Reformieren von Erdölkohlenwasserstoffen
DE60011135T2 (de) Verfahren zur herstellung von olefinen
DE102005053233A1 (de) Verfahren zur Aromatisierung von Nichtaromatischen Kohlenwasserstoffen mit Wasserdampf

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 08750114

Country of ref document: EP

Kind code of ref document: A1

DPE1 Request for preliminary examination filed after expiration of 19th month from priority date (pct application filed from 20040101)
DPE1 Request for preliminary examination filed after expiration of 19th month from priority date (pct application filed from 20040101)
NENP Non-entry into the national phase

Ref country code: DE

122 Ep: pct application non-entry in european phase

Ref document number: 08750114

Country of ref document: EP

Kind code of ref document: A1