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WO2003093205A2 - Procede de preparation d'hydrocarbures halogenes insatures et dispositif utilise a cet effet - Google Patents

Procede de preparation d'hydrocarbures halogenes insatures et dispositif utilise a cet effet Download PDF

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Publication number
WO2003093205A2
WO2003093205A2 PCT/EP2003/004505 EP0304505W WO03093205A2 WO 2003093205 A2 WO2003093205 A2 WO 2003093205A2 EP 0304505 W EP0304505 W EP 0304505W WO 03093205 A2 WO03093205 A2 WO 03093205A2
Authority
WO
WIPO (PCT)
Prior art keywords
reactor
gas
catalytically active
active material
permeable
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/EP2003/004505
Other languages
German (de)
English (en)
Other versions
WO2003093205A3 (fr
Inventor
Michael Benje
Horst Ertl
Ingolf Mielke
Thomas Wild
Peter Kammerhofer
Peter Schwarzmaier
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.)
Vinnolit Technologie GmbH and Co KG
ThyssenKrupp Industrial Solutions AG
Original Assignee
Uhde GmbH
Vinnolit Technologie GmbH and Co KG
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
Priority claimed from DE10219721A external-priority patent/DE10219721B4/de
Priority claimed from DE10252891A external-priority patent/DE10252891A1/de
Application filed by Uhde GmbH, Vinnolit Technologie GmbH and Co KG filed Critical Uhde GmbH
Priority to AU2003227694A priority Critical patent/AU2003227694A1/en
Publication of WO2003093205A2 publication Critical patent/WO2003093205A2/fr
Publication of WO2003093205A3 publication Critical patent/WO2003093205A3/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C17/00—Preparation of halogenated hydrocarbons
    • C07C17/25—Preparation of halogenated hydrocarbons by splitting-off hydrogen halides from halogenated 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
    • B01J12/00—Chemical processes in general for reacting gaseous media with gaseous media; Apparatus specially adapted therefor
    • B01J12/007—Chemical processes in general for reacting gaseous media with gaseous media; Apparatus specially adapted therefor in the presence of catalytically active bodies, e.g. porous plates
    • 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
    • B01J19/24—Stationary reactors without moving elements inside
    • B01J19/2415—Tubular reactors
    • B01J19/243—Tubular reactors spirally, concentrically or zigzag wound
    • 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
    • B01J38/00—Regeneration or reactivation of catalysts, in general
    • B01J38/04—Gas or vapour treating; Treating by using liquids vaporisable upon contacting spent catalyst
    • B01J38/10—Gas or vapour treating; Treating by using liquids vaporisable upon contacting spent catalyst using elemental hydrogen
    • 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
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/0207—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly horizontal
    • B01J8/0214—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly horizontal in a cylindrical annular shaped bed
    • 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
    • B01J2208/00654—Controlling the process by measures relating to the particulate material
    • B01J2208/00707—Fouling
    • 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
    • Y02P20/584—Recycling of catalysts

Definitions

  • the present invention relates to a method for producing unsaturated halogen-containing hydrocarbons from saturated halogen-containing hydrocarbons and to a device which is particularly suitable for carrying out the method.
  • a preferred process relates to the production of vinyl chloride (hereinafter also referred to as "NC”) from 1,2-dichloroethane (hereinafter also referred to as "DCE").
  • the process requires considerable amounts of energy for the various process steps, such as heating the DCE to the gap temperature, the reaction itself and the subsequent purification of the product mixture.
  • a group of measures aimed at improving the economics of the process aims at
  • cleavage promoters hereinafter also referred to as “promoters of thermal cleavage”. These are compounds which are among those found in the reactor
  • NS OPSE Conditions break down into radicals and intervene in the chain reaction that leads to the formation of the desired products.
  • the use of such compounds, which are added to the feed gas when they are introduced into the reactor, is known, for example, from US Pat. No. 4,590,318 or DE-A-3,328,691.
  • Combustion promoters added to the starting gas are used. Common to all these processes is that the reactor is filled with a sufficient amount of catalyst such that the gas mixture flowing through the reactor, which may contain gap promoters, comes into contact with the catalyst as completely as possible.
  • the educt in the reactor flows through a bed of
  • Catalyst and the complete amount of starting material is converted on the catalyst. Examples of such processes can be found in DE-A-2, 156,943, US-A-3,268,602 and WO-A-00 / 29,359.
  • WO-A-02 / 14,581 describes a dehydrochlorination of halogenated
  • phosphines are used as coking inhibitors.
  • the phosphine can be mixed into the feed gas or the reactor can be pretreated with the phosphine before starting operation.
  • the catalyst mainly turns into gap promoters Generates starter radicals, which promotes the subsequent thermal cleavage of the starting material.
  • An object of the present invention is to provide a pyrolysis process of halogen-containing aliphatic hydrocarbons with which larger conversions are possible compared to conventional processes at an otherwise identical operating temperature or with which a lowering of the operating temperature is possible compared to conventional processes with otherwise identical conversions.
  • the method according to the invention allows the use of gap promoters in such amounts that the selectivity of the reaction is not or not insignificantly deteriorated compared to methods without gap promoters.
  • the present invention relates to a process for the production of ethylenically unsaturated halogen-containing aliphatic hydrocarbons by thermal cleavage of saturated halogen-containing aliphatic hydrocarbons, comprising the measures: a) introducing a feed gas stream containing heated gaseous halogen-containing aliphatic hydrocarbons into a reactor which contains at least one on and / or in the interior a gas-permeable connected to a feed line for a promoter of the thermal cleavage
  • the method according to the invention is described using the DCE / VC system as an example. It is also suitable for the production of other halogen-containing unsaturated hydrocarbons from halogen-containing saturated hydrocarbons. All these reactions have in common that the cleavage is a radical chain reaction in which, in addition to the desired product, undesired by-products are formed, which lead to coking of the plants during continuous operation.
  • Any material, including metal alloys, which can be used under the conditions prevailing in the reactor can be used as the catalytically active material
  • catalytically active materials are metals or metal oxides.
  • catalytically active materials promote the radical formation process of the cracking promoter, which ultimately leads to an increased concentration of starter radicals and to an increased conversion in the cracking reaction without large amounts of the cracking promoter having to be added to the feed gas.
  • a metal or a metal alloy from subgroup 8 of the Periodic Table of the Elements in particular iron, cobalt, nickel, rhodium, ruthenium, palladium or platinum, and alloys of these metals with gold are preferably used as catalytically active material.
  • Rhodium, ruthenium palladium and platinum are very particularly preferred. All carriers known to the person skilled in the art can be used as the gas-permeable carrier, which can be attached to selected areas of the reactor inner wall and / or the reactor interior and which are provided with feed lines for the gap promoter. This can be a cage, which is formed, for example, by a grid or a perforated metal plate, the one
  • gas-permeable carrier can be a gas-permeable one
  • Act plate which is surrounded by a flat structure, such as a wire mesh, made of catalytically active material.
  • the gas-permeable carrier is preferably a porous molded body. This can consist of the catalytically active material and / or of another material. It is preferably a porous ceramic which is coated in particular with the catalytically active material, in particular with a metal; or it is a porous ceramic that is doped with the catalytically active material, in particular with a metal.
  • the catalytically active material can be applied in any form in or on the gas-permeable support. Such arrangements are known to the person skilled in the art.
  • the catalytically active material can be in the form of moldings with the largest possible surface-to-volume ratio.
  • the catalytically active material is preferably applied as a coating and / or as a doping on or in the gas-permeable carrier.
  • the arrangement and surface of the catalytically active material are to be selected such that the major part of the feed gas flowing through the reactor is in a thermal gas phase reaction is implemented, and the catalytically active material is mainly used to generate starter radicals for thermal conversion.
  • the ratio of catalyst surface to inner reactor surface is 10:90 or less. This ratio is preferably from 0.5: 99.5 to 10:90.
  • catalyst surface is to be understood as the outer geometric surface of the gas-permeable support.
  • reactor interior surface is to be understood as the geometric surface of the reactor interior.
  • a gaseous promoter of the thermal cleavage preferably diluted with an inert gas, is fed to the gas-permeable support or gas-permeable molded body through at least one supply line connected thereto, and is fed through the gas-permeable support to the catalytically active material or the catalytically active material consisting thereof.
  • a catalytically active metal arranged on and / or in the gas-permeable carrier is rinsed with a gaseous promoter of the thermal cleavage supplied through the gas-permeable carrier.
  • the feeding of the gap promoter or the flushing with the gap promoter can take place continuously or at predetermined time intervals.
  • the gap promoter can be fed undiluted or together with inert gases such as nitrogen and / or noble gases. Dilution with inert gases is particularly advisable when continuously supplying a gap promoter, since it is known that high partial pressures of the reaction product VC or of by-products that are precursors of coke formation (acetylene, benzene) near metal surfaces lead to accelerated coking.
  • inert gases such as nitrogen and / or noble gases.
  • the temperature of the gap promoter supplied via the gas-permeable carrier is expediently adapted to the temperature which is in the interior of the reactor
  • the location of the gas-permeable carrier prevails. This can be done, for example, by a heating device attached outside the reactor.
  • Promoters of the pyrolysis reaction are known per se. These are usually halogen-containing, preferably chlorine-containing compounds or molecular oxygen. Examples of this can be found in the already mentioned US-A-4,590,318 and DE-A-3,328,691. Under the special conditions of the method according to the invention e.g. DCE should also be considered as a promoter of the pyrolysis reaction, since this disintegrates on the catalytically active surfaces used.
  • Preferred promoters of the pyrolysis reaction are molecular chlorine, nitrosyl chloride, trichloroacetyl chloride, chloral, hexachloroacetone, benzotrichloride, monochloromethane, dichloromethane, trichloromethane, carbon tetrachloride or hydrogen chloride.
  • a preferred example of this is hydrogen or a mixture of hydrogen with inert gases.
  • the supply of the gaseous reducing agent can take place via the gas-permeable carrier, either via the same
  • a catalytically active metal arranged on or in the gas-permeable carrier or present as a gas-permeable shaped body is flushed with a gaseous reducing agent, preferably with hydrogen, supplied through the gas-permeable carrier or the shaped body.
  • the flushing with the gaseous reducing agent can take place continuously or at predetermined time intervals.
  • the gaseous reducing agent can be added undiluted or together with inert gases such as nitrogen and / or noble gases.
  • the temperature of the gaseous reducing agent is expediently adapted to the temperature which prevails in the interior of the reactor at the location of the gas-permeable support.
  • Flushing with reducing agent can efficiently prevent or slow down the coking of the surface of the catalytically active material, thereby extending the operating time of the cracking furnace and further increasing the turnover of the cracking reaction.
  • the operation of the reactor is not interrupted during the rinsing process.
  • the feed of the gap promoter to the gas-permeable support or molded body and its supply to the catalytically active material can take place together with the gaseous reducing agent or separately from it in time and / or space.
  • At least one is preferably arranged on a gas-permeable carrier or in the form of a gas-permeable shaped body catalytically active material in the vicinity of the entry of the feed gas stream into the reactor.
  • the feed gas stream comes into contact with one or more candles made of porous ceramic during passage in the reactor, on the surface of which there is in each case a catalytically active metal layer and / or which is doped with catalytically active metal.
  • the number of candles in the first third of the reactor is very particularly preferably greater than in the second third and / or in the third third.
  • the method according to the invention can be operated using the usual pressures and / or temperatures.
  • Common operating pressures are in the range of 0.8 to 4 MPa (furnace inlet);
  • Common operating temperatures are in the range from 450 to 550 ° C (furnace exit) and in the range from 250 to 350 ° C (furnace entrance).
  • the endothermic cleavage reaction requires a constant supply of energy; this takes place when the gas to be split passes through the reactor.
  • Another embodiment of the process according to the invention relates to the thermal cracking of the product gas in an adiabatic post-reactor downstream of the reactor, comprising the measures: d) introducing the product gas stream containing heated halogen-containing aliphatic hydrocarbon, hydrogen halide and ethylenically unsaturated halogen-containing aliphatic hydrocarbon from the reactor into an adiabatic post-reactor, in which the reaction using the heat supplied by the product gas stream with cooling of the product gas is continued, and which preferably has at least one catalytically active material arranged on and / or in a gas-permeable support or in the form of a gas-permeable shaped body, and e) optionally supplying a gaseous promoter of the thermal
  • the process according to the invention can only include measures d) and e) in the adiabatic post-reactor without using an upstream reactor which has at least one catalytically active material arranged on and / or in a gas-permeable support.
  • the method according to the invention with measures d) and e) in the adiabatic post-reactor is preferred and is combined with the use of an upstream reactor which has at least one catalytically active material arranged on and / or in a gas-permeable support.
  • the invention also relates to a reactor for carrying out the process defined above, comprising the elements: i) feed line for the feed gas stream containing saturated halogen-containing aliphatic hydrocarbon opening into the reactor, ii) at least one arranged on and / or in a gas-permeable carrier or in the form of a gas-permeable one Shaped body present catalytically active material, which is attached to the inside of the reactor, iii) connected to the gas-permeable support or shaped body
  • Supply line for a gas containing cracking promoters iv) heating device for heating the gas containing cracking promoters, v) heating device for heating and / or maintaining the temperature of the gas stream in the reactor, and vi) discharge leading from the reactor for the product gas stream of the thermal cleavage containing ethylenically unsaturated halogen-containing aliphatic hydrocarbon.
  • a tubular reactor is preferred.
  • the reactor according to the invention can be followed by an adiabatic post-reactor which preferably contains the elements ii), iii) and iv) defined above.
  • the required heat of reaction is supplied by the heat of the product gas stream supplied, which cools down as a result.
  • an adiabatic post-reactor can also be connected to a reactor known per se which has the
  • the gas-permeable carrier is preferably a porous molded body, in particular made of porous ceramic.
  • the porous ceramic is in the form of a candle, the surface of which is coated with catalytically active material, in particular metal, and / or which is doped with catalytically active metal, and the candle is provided with a feed line for the Gap promoter equipped for forwarding to the catalytically active material.
  • FIG. 1 A preferred gas-permeable support with catalytically active material arranged thereon shown in longitudinal section
  • Figure 2 Another preferred gas-permeable support with catalytically active material arranged thereon shown in longitudinal section
  • Figure 3 tubular reactor with support according to Figure 1 or 2 in longitudinal section
  • the feed gas stream comes with one or more as it passes through the reactor
  • a cylindrical, porous molded body (3) which is provided on the inside with a catalytically active layer (4), is clamped in an outer tube (1) by means of two opposing covers or flanges (2).
  • the arrangement of the shaped body (3) in the outer tube (1) forms a jacket space (5) and an interior (6), the jacket space (5) on the end faces of the covers or flanges (2) against the interior (6) and is sealed against the outer tube (1).
  • a gas (16) containing gap promoters is introduced into the jacket space (5) and flows into the interior (6) through the cylindrical, porous molded body (3).
  • the shaped body (3) in the outer tube (1) can also be used with the outer tube in other ways, for example by means of a suitable choice of material
  • Screwing and / or welding to be connected so that the jacket space (5) and the interior (6) form in such a way that the jacket space (5) is sealed against the interior (6) and against the outer tube (1).
  • FIG. 2 Such a device is shown in Figure 2.
  • a cylindrical, porous molded body (3) provided on the inside with a layer of catalytically active material (4) is welded to an outer tube (1) on its end faces.
  • a jacket space (5) and an interior (6) is formed, the jacket space (5) being sealed off from the interior (6) and from the outer tube (1).
  • the invention also relates to a reactor containing at least one such device for carrying out the process defined above and a process for producing ethylenically unsaturated halogen-containing aliphatic hydrocarbons by thermal cracking of saturated halogen-containing aliphatic hydrocarbons, in which such a reactor is used.
  • the molded body (3) preferably has the same inside diameter or the same free cross section as the upstream, intermediate or downstream reaction tube.
  • the cylindrical, porous molded body (3) can consist of sintered metal, porous ceramic or another, porous and temperature-resistant material.
  • the porous hollow body (3) consists of zirconium oxide.
  • the layer of catalytically active material can be applied to the inside of the porous shaped body in various ways, e.g. by vapor deposition,
  • Sputtering galvanic or electroless metal deposition, impregnation, precipitation (impregnation) or combinations of these methods.
  • the type of application of the catalytically active layer is not restricted to the methods listed here.
  • the cylindrical, porous shaped body (3) can also or additionally be doped with the catalytically active material.
  • the jacket space (5) can be sealed off from the interior (6) by means of a
  • a spring (8) is worked out from the end face of the cylindrical, porous molded body, which presses or cuts into the seal (7).
  • the end face or the section of the cylindrical, porous shaped body (3) immediately adjacent to the end face can, if it consists of ceramic material, be sealed with a so-called glass solder or a temperature-resistant ceramic adhesive.
  • the jacket space (5) is preferably sealed off from the outside by means of seals (13).
  • Spacers (9, 10, 11) incorporated into the end face of the cover or the flanges ensure a defined surface pressure of the seals (8, 13, 14) and protect the cylindrical, porous molded body (3) against breakage.
  • the seal (7) can be a metal seal or a seal made of another temperature-resistant and sufficiently soft material. A metal seal is preferred.
  • the seals (13) and (14) are seals made of a temperature-resistant material, such as made of graphite, asbestos or asbestos substitutes. Other temperature-resistant materials can also be used.
  • the seals (13) and (14) can also be welding lip seals.
  • the seals (13) and (14) can also be combinations of an internal seal made of a soft and temperature-resistant material and an external welding lip seal.
  • the cylindrical, porous shaped body (3) is a break-resistant material, such as sintered metal, it can also be screwed or welded to the covers (2).
  • an arrangement is preferred in which the cylindrical, porous molded body (3) is welded to one of the covers or flanges (2) and screwed to the other cover (flange), so that the cylindrical, porous molded body (3 ) z. B. can be easily dismantled for cleaning and regeneration purposes.
  • An arrangement is very particularly preferred in which cylindrical connecting parts or intermediate pieces made of solid material of the same inside and outside diameter are welded onto both ends of the cylindrical, porous molded body (3), provided that this consists of metallic sintered material, e.g. can be provided with threaded holes for screwing on flanges, or to which the flanges can be welded directly.
  • the jacket space is sealed off from the interior by a seal between the cylindrical, porous molded body (3) and the cover or flange (2).
  • the preheated feed gas stream (15) flows through the device described.
  • the reactor outlet gas mixture flows through it.
  • the initiated cleavage promoter (16) at least partially breaks down into radicals on the catalytically active material, which in turn promote the progress of the radical chain reaction.
  • the cylindrical, porous shaped body (3) is from the outside inwards by one
  • Gas (16) containing gap promoters which can optionally be diluted with inert gas, flows through.
  • the gas (mixture) is introduced into the jacket space (5) from the outside through an inlet opening through a feed line, not shown and flows through the cylindrical, porous molded body (3) and the catalytically active layer (4) into the interior (6) of the device.
  • shaped bodies (3) of catalytically active layer (4) must be designed and arranged in such a way that a gas flow which is as uniform as possible is made possible through these layers and that no zones are formed which are not flowed through by gas.
  • the device shown in Figures 1 and 2 can be installed in a conventional tubular reactor for the production of ethylenically unsaturated halogen-containing aliphatic hydrocarbons by thermal cleavage of saturated halogen-containing aliphatic hydrocarbons.
  • FIG. 3 Such an installation is shown schematically in FIG. 3.
  • the tubular reactor comprises an oven and a reaction tube.
  • an oven fired with a primary energy source is divided into a so-called radiation zone (16) and a convection zone (17).
  • the heat required for the pyrolysis is transferred to the reaction tube primarily by radiation from the furnace walls heated by the burner.
  • Radiation zone exiting smoke gases used by convective heat transfer is achieved.
  • the starting material of the pyrolysis reaction e.g. EDC, _heated, evaporated or overheated. It is also possible to generate water vapor and / or preheat combustion air.
  • liquid EDC is first preheated in the convection zone of the cracking furnace and then evaporated in a special evaporator outside the cracking furnace.
  • the vaporous EDC is then again fed to the convection zone and superheated there, the pyrolysis reaction already being able to start. After overheating, the EDC enters the radiation zone, where the conversion to vinyl chloride and hydrogen chloride takes place.
  • the cracking furnace is expanded by two additional, non-heated compartments (18) which can be thermally insulated. From the actual radiation or
  • Convection zone (16, 17) loops of the reaction tube are then passed through these compartments (18).
  • the devices according to FIG. 1 or 2 (19) containing devices for introducing a gap promoter and catalytically active elements are then mounted, that is to say built into the reaction tube, so that the
  • Educt gas flow can flow through the reaction tube and interior (6) of the device.
  • the loops of the reaction tube which are led from the radiation or convection zone (16, 17) into the unheated compartments (18) are preferably provided with thermal insulation.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Physics & Mathematics (AREA)
  • Fluid Mechanics (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

La présente invention concerne un procédé de préparation d'hydrocarbures aliphatiques halogénés éthyléniquement insaturés, par craquage thermique d'hydrocarbures aliphatiques halogénés saturés. A cet effet, on fait passer un courant d'éduit gazeux par un réacteur qui présente en son intérieur au moins un matériau actif du point de vue catalytique disposé sur un support perméable aux gaz relié à une conduite d'amenée, ou un corps moulé en matériau actif du point de vue catalytique, perméable aux gaz et relié à celui-ci, par lequel un promoteur de craquage est introduit dans le réacteur. Le procédé permet d'obtenir un meilleur taux de conversion de la réaction de craquage.
PCT/EP2003/004505 2002-05-02 2003-04-30 Procede de preparation d'hydrocarbures halogenes insatures et dispositif utilise a cet effet Ceased WO2003093205A2 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AU2003227694A AU2003227694A1 (en) 2002-05-02 2003-04-30 Method for the production of unsaturated hydrocarbons containing halogen and suitable device therefor

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
DE10219721.0 2002-05-02
DE10219721A DE10219721B4 (de) 2002-05-02 2002-05-02 Verfahren zur Herstellung ungesättigter halogenhaltiger Kohlenwasserstoffe sowie dafür geeignete Vorrichtung
DE10252891A DE10252891A1 (de) 2002-11-12 2002-11-12 Verfahren zur Herstellung ungesättigter halogenhaltiger Kohlenwasserstoffe sowie dafür geeignete Vorrichtung
DE10252891.8 2002-11-12

Publications (2)

Publication Number Publication Date
WO2003093205A2 true WO2003093205A2 (fr) 2003-11-13
WO2003093205A3 WO2003093205A3 (fr) 2004-09-02

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WO2020048556A1 (fr) * 2018-09-05 2020-03-12 Wandzik Christoph Gregor Réacteur à hydrogène et le procédé de chimie régéneratif
WO2020163169A1 (fr) * 2019-02-05 2020-08-13 Saudi Arabian Oil Company Production de gaz synthétique

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EP0728831B1 (fr) * 1995-02-17 2000-07-12 Linde Aktiengesellschaft Procédé et appareillage pour le craquage d'hydrocarbures

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2020048556A1 (fr) * 2018-09-05 2020-03-12 Wandzik Christoph Gregor Réacteur à hydrogène et le procédé de chimie régéneratif
WO2020163169A1 (fr) * 2019-02-05 2020-08-13 Saudi Arabian Oil Company Production de gaz synthétique

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