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WO2008034837A1 - Procédé pour produire du 1,2-dichloréthane par oxychloration catalytique d'éthylène dans un réacteur à lit fluidisé - Google Patents

Procédé pour produire du 1,2-dichloréthane par oxychloration catalytique d'éthylène dans un réacteur à lit fluidisé Download PDF

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Publication number
WO2008034837A1
WO2008034837A1 PCT/EP2007/059871 EP2007059871W WO2008034837A1 WO 2008034837 A1 WO2008034837 A1 WO 2008034837A1 EP 2007059871 W EP2007059871 W EP 2007059871W WO 2008034837 A1 WO2008034837 A1 WO 2008034837A1
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WO
WIPO (PCT)
Prior art keywords
fluidized bed
internals
cells
bed reactor
reactor
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.)
Ceased
Application number
PCT/EP2007/059871
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German (de)
English (en)
Inventor
Lothar Seidemann
Andreas Kern
Heiko Urtel
Henrik Junicke
Dieter Stützer
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
BASF SE
Original Assignee
BASF SE
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Filing date
Publication date
Application filed by BASF SE filed Critical BASF SE
Publication of WO2008034837A1 publication Critical patent/WO2008034837A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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    • 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
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/1872—Details of the fluidised bed reactor
    • 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
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/32—Packing elements in the form of grids or built-up elements for forming a unit or module inside the apparatus for mass or heat transfer
    • 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
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/005—Separating solid material from the gas/liquid stream
    • 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
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/1836—Heating and cooling the reactor
    • 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
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
    • B01J8/34—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with stationary packing material in the fluidised bed, e.g. bricks, wire rings, baffles
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C17/00—Preparation of halogenated hydrocarbons
    • C07C17/093—Preparation of halogenated hydrocarbons by replacement by halogens
    • C07C17/15—Preparation of halogenated hydrocarbons by replacement by halogens with oxygen as auxiliary reagent, e.g. oxychlorination
    • C07C17/152—Preparation of halogenated hydrocarbons by replacement by halogens with oxygen as auxiliary reagent, e.g. oxychlorination of hydrocarbons
    • C07C17/156—Preparation of halogenated hydrocarbons by replacement by halogens with oxygen as auxiliary reagent, e.g. oxychlorination of hydrocarbons of unsaturated hydrocarbons
    • 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
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00115—Controlling the temperature by indirect heat exchange with heat exchange elements inside the bed of solid particles
    • B01J2208/00132—Tubes
    • 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
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00115—Controlling the temperature by indirect heat exchange with heat exchange elements inside the bed of solid particles
    • B01J2208/0015—Plates; Cylinders
    • 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
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/32—Details relating to packing elements in the form of grids or built-up elements for forming a unit of module inside the apparatus for mass or heat transfer
    • B01J2219/322—Basic shape of the elements
    • B01J2219/32203—Sheets
    • B01J2219/3221—Corrugated sheets
    • 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
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/32—Details relating to packing elements in the form of grids or built-up elements for forming a unit of module inside the apparatus for mass or heat transfer
    • B01J2219/322—Basic shape of the elements
    • B01J2219/32203—Sheets
    • B01J2219/32213—Plurality of essentially parallel sheets
    • B01J2219/3222—Plurality of essentially parallel sheets with sheets having corrugations which intersect at an angle different from 90 degrees
    • 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
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/32—Details relating to packing elements in the form of grids or built-up elements for forming a unit of module inside the apparatus for mass or heat transfer
    • B01J2219/322—Basic shape of the elements
    • B01J2219/32203—Sheets
    • B01J2219/32224—Sheets characterised by the orientation of the sheet
    • B01J2219/32227—Vertical orientation
    • 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
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/32—Details relating to packing elements in the form of grids or built-up elements for forming a unit of module inside the apparatus for mass or heat transfer
    • B01J2219/324—Composition or microstructure of the elements
    • B01J2219/32408—Metal

Definitions

  • the invention relates to a process for the preparation of 1, 2-dichloroethane by catalytic oxychlorination of ethene in a fluidized bed reactor.
  • the oxychlorination of ethene for the preparation of 1, 2-dichloroethane is a known technical process and is usually carried out on a catalyst, in particular a catalyst containing copper in the active composition, preferably copper chloride, and which is preferably supported.
  • the reaction is exothermic and is carried out at elevated temperature, typically in the range of 220 to 245 0 C and elevated pressure, typically from 150 to 500 kPas. At these reaction conditions, copper chloride is volatile, with the result that the catalyst activity decreases over time.
  • additives which reduce the volatility of copper chloride.
  • additives are, for example, alkali metal chlorides, in particular potassium chloride and cesium chloride, alkaline earth metal chlorides, in particular magnesium chloride, chlorides of rare earth metals, in particular cerium chloride or compounds of the platinum group metals, preferably of ruthenium and / or a gold compound.
  • a process for oxychlorination in a fluidized bed reactor is described at ww.oxyvinyls.com.
  • the reaction is carried out in a fluidized-bed reactor, which typically consists of a cylindrical vessel equipped with a gas distribution system, which ensures uniform fluidization and equal distribution of ethene, hydrogen chloride and oxygen.
  • a gas distribution system which ensures uniform fluidization and equal distribution of ethene, hydrogen chloride and oxygen.
  • To minimize the discharge of fluidized catalyst particles from the reactor usually cyclone are used.
  • the heat of reaction in this case can be done either by evaporation of cooling water or by other heat transfer media, which can be performed in particular by cooling coils.
  • Oxychlorination catalysts tend to sticking when used in fluidized beds, which promotes continuity of the reaction, and fluidized catalysts for the oxychlorination of ethene to 1, 2-dichloroethane need not only be optimized for activity and selectivity, but also for sticking "-Free vortex behavior exhibit.
  • Such catalyst compositions are proposed, for example, in DE-A 102 04 608.5, containing 3 to 12% by weight of copper as copper salt, 0 to 3% by weight of an alkaline earth metal as alkaline earth metal salt, 0 to 3% by weight of an alkali metal as alkali metal salt and 0.001 to 0.1 wt .-%, preferably 0.005 to 0.05 wt .-%, of at least one metal selected from the group of ruthenium, rhodium, palladium, osmium, iridium and platinum and / or 0.0001 to 0 , 1 wt .-%, preferably 0.001 to 0.05 wt .-% gold, as the corresponding metal salt or tetrachloroauric acid.
  • the object is achieved by a process for the preparation of 1, 2-dichloroethane by catalytic oxychlorination of ethene in a fluidized bed reactor, wherein a gaseous reaction mixture containing ethene, hydrogen chloride and oxygen, flows through a heterogeneous, particulate, a fluidized bed catalyst from bottom to top characterized in that internals are arranged in the fluidized bed, which divide the fluidized bed into a plurality of horizontally and a plurality of vertically arranged in the fluidized bed reactor cells, with cell walls that are gas permeable and have the openings having an exchange number of the heterogeneous particulate Ensure catalyst in the vertical direction in the range of 1 to 100 liters / hour per liter of reactor volume.
  • the known catalysts for oxychlorination can be used, in particular catalysts containing copper and next to one or more promoters, especially alkali metal chlorides, preferably potassium chloride or cesium chloride, alkaline earth metal chlorides, preferably magnesium chloride and / or chlorides of rare earth metals, preferably Cerium chloride, and / or salts of platinum metals, preferably of ruthenium and / or a gold compound.
  • alkali metal chlorides preferably potassium chloride or cesium chloride
  • alkaline earth metal chlorides preferably magnesium chloride and / or chlorides of rare earth metals, preferably Cerium chloride, and / or salts of platinum metals, preferably of ruthenium and / or a gold compound.
  • the cell walls are gas permeable and have openings which in the vertical direction in the fluidized bed reactor a solid - Allow mass transfer.
  • openings can be provided in the cell walls, which allow a solid exchange in the horizontal direction.
  • the exchange number is determined by the use of radioactively labeled solid-tracer particles which are introduced into the fluidizing reaction system, such as in: G. Reed “Radioisotope techniques for problem-solving in industrial process plants", Chapter 9 ("Measurement of residence times and residence-time distribution "), p. 112-137, (J.S. Charlton, ed.), Leonard Hill, Glasgow and London 1986, (ISBN 0-249-44171-3). By recording the time and place of these radioactively labeled particles, the solids movement can be determined locally and the exchange number can be deduced (G.
  • the residence time of the heterogeneous particulate catalyst in the same can be adapted to the characteristics of each reaction to be performed.
  • the backmixing is limited and thus improving the selectivity and the conversion.
  • the capacity the reactor can be adjusted as needed.
  • the capacity of the reactor according to the invention is thus not limited and can be adapted to the specific needs, for example, for reactions on a large scale.
  • the cell material itself occupies only a limited portion of the cross-section of the fluidized bed reactor, in particular only about 1 to 10% of the cross-sectional area of the fluidized bed reactor and therefore does not lead to those in the packers known from the prior art, associated with increased cross-sectional occupancy disadvantages.
  • the fluidized bed reactor used in the process according to the invention is, as usual, pressurized with the gaseous starting materials from below via a gas distributor. As the reaction zone passes, the gaseous feedstocks on the heterogeneous particulate catalyst, which is excited by the gas flow to swirl, are partially reacted. The partially reacted feedstocks flow into the next cell, where they are further partially reacted.
  • a Feststoffabscheidevorraum is provided which separates entrained catalyst from the gas phase.
  • the reacted product leaves the fluidized bed reactor according to the invention at the upper end of the same solids.
  • fluidized-bed reactor used in accordance with the invention can additionally be acted upon with liquid educts both from below and from the side. However, these must be able to evaporate directly at their point of addition to ensure the fluidity of the catalyst.
  • the cells are not limited in their geometry; it may, for example, be cells with round walls, in particular hollow spheres, or even cells with angular walls. In the case of an angular formation of the walls, it is preferred that the cells have not more than 50 corners, preferably no more than 30 and in particular no more than 10 corners.
  • the cell walls in the cells of the internals are gas-permeable, in order to ensure by swirling through the gas phase through the cells, the swirling of the heterogeneous particulate catalyst.
  • the cell walls may be formed of a screen fabric or of sheet-like materials, for example, have round or otherwise shaped holes.
  • the average mesh size of the mesh fabrics used or the preferred width of the holes in the cell walls is in particular between 50 and 1 mm, more preferably between 10 and 1 mm and particularly preferably between 5 and 1 mm.
  • Cross-channel packings are particularly preferably used as internals in the fluidized bed, that is, packings with kinked, gas-permeable metal plates, expanded metal or fabric layers arranged in parallel in the vertical direction in the fluidized bed reactor, with kinked edges forming buckling surfaces with a non-zero angle of inclination to the vertical, and the buckling surfaces of successive metal sheets, expanded metal or fabric layers have the same angle of inclination, but with opposite signs and thereby form cells which are delimited in the vertical direction by constrictions between the bending edges.
  • cross-channel packings are packings of the types Mellpack ®, CY or BX from. Sulzer AG, CH-8404 Winterthur or types A3, BSH, B1 or M of Messrs. Monz GmbH, D-40723 Hilden.
  • cross-channel packages are formed in the vertical direction between two successive metal sheets, expanded metal or fabric layers, the kinked structuring of the same, cavities, that is, cells, which are limited by bottlenecks between the creases.
  • the mean hydraulic diameter of the cells is preferably in the range between 500 and 1 mm, more preferably between 100 and 5 mm and particularly preferred between 50 and 5 mm.
  • the average height of the cells is preferably between 100 and 1 mm, more preferably between 100 and 3 mm and particularly preferably between 40 and 5 mm.
  • cross-channel packings occupy only a small part of the cross-sectional area of the fluidized-bed reactor, in particular a proportion of about 1 to 10% thereof.
  • the inclination angle of the buckling surfaces to the vertical in the range of 10 to 80 °, in particular between 20 and 70 °, more preferably between 30 and 60 °.
  • the buckling surfaces in the metal sheets, expanded metal or fabric layers preferably have a buckling height in the range between 100 and 3 mm, particularly preferably between 40 and 5 mm, and a distance of the bottlenecks between the bending edges in the range between 50 and 2 mm, particularly preferably between 20 and 3 mm, on.
  • the heat exchangers may for example be plate-shaped or tubular and be arranged vertically, horizontally or inclined in the fluidized bed reactor.
  • the heat transfer surfaces can be tailored to the specific reaction; As a result, each reaction can be implemented thermally with the reactor concept according to the invention.
  • the cell-forming internals are preferably made of materials with very good thermal conductivity, so that the heat transfer through the cell walls is not hindered.
  • the heat transfer properties of the reactor according to the invention correspond to those of a conventional fluidized bed reactor.
  • the materials for the cell-forming internals should also have sufficient stability under reaction conditions; In particular, in addition to the resistance to chemical and thermal stresses, the resistance of the material to mechanical attack by the swirling catalyst should also be taken into account.
  • metal, ceramic, polymer or glass materials are particularly suitable.
  • the internals are preferably designed such that they divide 10 to 90 vol .-% of the fluidized bed into cells.
  • the lower region of the fluidized bed is preferably free in the throughflow direction of the gaseous reaction mixture of internals.
  • the internals which divide the fluidized bed in cells, o- arranged above the heat exchanger are provided.
  • the reactor according to the invention has no disadvantages with respect to segregation and output tendency of the swirling particulate catalyst.
  • Figure 1 is a schematic representation of a preferred embodiment of a fluidized bed reactor used in the invention.
  • Figure 2 is a schematic representation of a preferred embodiment of inventions used internals.
  • the fluidized-bed reactor 1 shown in FIG. 1 comprises a solids-free gas distribution zone 2, internals 3, which form cells 4, with a heat exchanger 5 in the region of the internals 3.
  • the reactor widens, and has at least one solids separator 6.
  • the arrow 7 indicates the supply of the gaseous starting materials and the arrow 8 indicates the removal of the gaseous product stream. Additional liquid-phase educts can be added laterally, via the dashed arrows 9.
  • Figure 2 illustrates a preferred embodiment of internals 3 according to the invention in the form of a cross-channel packing, with bent metal sheets 10 which are arranged parallel to each other in the longitudinal direction, with bending edges 11 which divide the metal sheet 10 into buckling surfaces 12 and wherein two successive metal sheets are arranged in that they have the same angle of inclination but with opposite signs and thereby form cells 4 bounded in the vertical direction by constrictions 13.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)

Abstract

L'invention concerne un procédé pour produire du 1,2-dichloréthane par oxychloration catalytique d'éthylène dans un réacteur à lit fluidisé. Selon l'invention, un mélange réactionnel gazeux contenant de l'éthylène, du chlorure d'hydrogène et de l'oxygène traverse de bas en haut un catalyseur hétérogène se présentant sous la forme de particules et formant un lit fluidisé. Cette invention est caractérisée en ce que ledit lit fluidisé comporte des éléments d'insertion qui divisent le lit fluidisé en une pluralité de cellules horizontales et verticales, les parois de ces cellules étant perméables aux gaz et comportant des ouvertures qui garantissent un échange des particules de catalyseur hétérogène dans la direction verticale de l'ordre de 1 à 100 litre(s)/heure par litre de volume du réacteur.
PCT/EP2007/059871 2006-09-19 2007-09-19 Procédé pour produire du 1,2-dichloréthane par oxychloration catalytique d'éthylène dans un réacteur à lit fluidisé Ceased WO2008034837A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
EP06120888 2006-09-19
EP06120888.0 2006-09-19

Publications (1)

Publication Number Publication Date
WO2008034837A1 true WO2008034837A1 (fr) 2008-03-27

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PCT/EP2007/059871 Ceased WO2008034837A1 (fr) 2006-09-19 2007-09-19 Procédé pour produire du 1,2-dichloréthane par oxychloration catalytique d'éthylène dans un réacteur à lit fluidisé

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Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4368173A (en) * 1979-09-12 1983-01-11 Instituto Mexicano Del Petroleo Reactor for oxichlorination of ethylene and process therefor
US5227548A (en) * 1988-12-20 1993-07-13 Imperial Chemical Industries Plc Oxychlorination of ethylene to 1,2-dichloroethane
EP0997187A1 (fr) * 1998-10-28 2000-05-03 Krupp Uhde GmbH Réacteur à lit fluidisé pour l'oxychloruration d'éthylène, oxygène et HCl
DE10204608A1 (de) * 2002-02-05 2003-08-07 Basf Ag Katalysatorzusammensetzung zur Oxychlorierung

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4368173A (en) * 1979-09-12 1983-01-11 Instituto Mexicano Del Petroleo Reactor for oxichlorination of ethylene and process therefor
US5227548A (en) * 1988-12-20 1993-07-13 Imperial Chemical Industries Plc Oxychlorination of ethylene to 1,2-dichloroethane
EP0997187A1 (fr) * 1998-10-28 2000-05-03 Krupp Uhde GmbH Réacteur à lit fluidisé pour l'oxychloruration d'éthylène, oxygène et HCl
DE10204608A1 (de) * 2002-02-05 2003-08-07 Basf Ag Katalysatorzusammensetzung zur Oxychlorierung

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