WO2003093206A1 - 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
WO2003093206A1
WO2003093206A1 PCT/EP2003/004506 EP0304506W WO03093206A1 WO 2003093206 A1 WO2003093206 A1 WO 2003093206A1 EP 0304506 W EP0304506 W EP 0304506W WO 03093206 A1 WO03093206 A1 WO 03093206A1
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WO
WIPO (PCT)
Prior art keywords
reactor
gas
heated
halogen
containing aliphatic
Prior art date
Application number
PCT/EP2003/004506
Other languages
German (de)
English (en)
Inventor
Michael Benje
Horst Ertl
Ingolf Mielke
Thomas Wild
Peter Kammerhofer
Peter Schwarzmaier
Original Assignee
Uhde Gmbh
Vinnolit Technologie Gmbh & 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 DE2002119722 external-priority patent/DE10219722B4/de
Priority claimed from DE2003107193 external-priority patent/DE10307193A1/de
Application filed by Uhde Gmbh, Vinnolit Technologie Gmbh & Co. Kg filed Critical Uhde Gmbh
Priority to AU2003233203A priority Critical patent/AU2003233203A1/en
Publication of WO2003093206A1 publication Critical patent/WO2003093206A1/fr

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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
    • 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
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/26—Nozzle-type reactors, i.e. the distribution of the initial reactants within the reactor is effected by their introduction or injection through nozzles
    • 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
    • B01J6/00—Heat treatments such as Calcining; Fusing ; Pyrolysis
    • B01J6/008—Pyrolysis reactions
    • 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
    • B01J8/06—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 in tube reactors; the solid particles being arranged in tubes
    • B01J8/062—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 in tube reactors; the solid particles being arranged in tubes being installed in a furnace
    • 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
    • B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
    • B01J2208/00212—Plates; Jackets; 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
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00504—Controlling the temperature by means of a burner
    • 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
    • B01J2208/0053—Controlling multiple zones along the direction of flow, e.g. pre-heating and after-cooling
    • 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
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00051—Controlling the temperature
    • B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
    • B01J2219/00119—Heat exchange inside a feeding nozzle or nozzle 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
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00051—Controlling the temperature
    • B01J2219/00132—Controlling the temperature using electric heating or cooling elements
    • B01J2219/00135—Electric resistance heaters
    • 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
    • B01J23/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals of the platinum group metals

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
  • a process for the dehydrochlorination of aliphatic hydrocarbons is known from WO-A-00 / 29,359, in which supported catalysts are used.
  • the reactor is filled with a sufficient amount of catalyst such that the gas mixture flowing through the reactor comes into contact with the catalyst as completely as possible.
  • the starting material in the reactor flows through a bed of the catalyst and the entire amount of starting material is converted on the catalyst.
  • An object of the present invention is to provide a pyrolysis Process of halogen-containing aliphatic hydrocarbons with which increased product yields are possible compared to conventional processes at otherwise the same operating temperature or with which a lowering of the operating temperature is possible compared to conventional processes with otherwise identical product yields.
  • the present invention relates to a process for producing 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 hydrocarbon into a reactor, in the interior of which at least one feed line for a heated gas opens, b) introducing a heated gas through the opening into the reactor
  • the temperature of the heated gas being higher than the temperature of the feed gas stream at the point of the mouth of the supply line, the total amount of the heated gas introduced into the reactor being not more than 10% by weight, based on the total mass flow in the reactor, and c) setting such a pressure and such a temperature inside the reactor so that hydrogen halide and ethylenically unsaturated halogen-containing aliphatic hydrocarbon are formed by thermal cracking of the halogen-containing aliphatic hydrocarbon.
  • 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 ones unsaturated hydrocarbons from halogenated 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 in continuous operation.
  • Any gas which is inert under the prevailing reaction conditions can be used as the heated gas for introduction into the feed gas stream via the feed line.
  • inert gases examples include nitrogen or noble gases, in particular argon, and carbon dioxide or hydrogen chloride.
  • the supplied gas is preferably only heated shortly before it is injected into the feed gas stream.
  • Typical temperatures of the supplied gas range from 500 to 1500 ° C, preferably 500 to 1000 ° C.
  • Typical temperatures of the educt gas flow are in the range from 250 to 500 ° C.
  • Temperature also depends on the nature of the gas and its quantity. According to the invention, a total of not more than 10% by weight, preferably not more than 5% by weight, particularly preferably 0.0005 to 5% by weight, based on the total mass flow in the reactor, is added.
  • more than 90%, preferably more than 95%, of the required heat of reaction is supplied by heating the reactor walls, while that by the hot gas supplied heat only serves to initiate and accelerate the reaction.
  • shock-like heating of a limited amount of the reactant gas promotes the radical chain reaction in the reactant gas, which ultimately leads to an increased concentration of radicals and an increased conversion in the cleavage reaction.
  • All devices known to the person skilled in the art for this purpose can be used as supply lines for the heated gas. Examples of this are pipelines which open into the reactor and which preferably have a nozzle at their end on the reactor side. According to the invention, the feed lines have a heating device for the heated gas immediately before their end on the reactor side.
  • the mouth of the feed lines can be in the reactor wall.
  • the feed lines preferably open into the interior of the reactor, in particular into the middle of the gas flow in the reactor, so that the heated gas does not come into contact with the reactor walls if possible.
  • the gas to be introduced is electrically heated in the feed line immediately before it is introduced into the reactor.
  • the heated gas is introduced into the reactor via one or more feed lines which are provided with porous ceramic candles at their end on the reactor side.
  • the candles are equipped on the inside with a heating device, for example with a heating cartridge installed inside, and allow the gas to be heated immediately before it is introduced into the reactor.
  • Plasmas which are preferably adjusted to the above-mentioned temperature ranges with inert gases; or the use of chemical reactions to generate heat, such as catalytic conversion or Combustion of chlorine with hydrogen shortly before the point where the feed pipe meets the reactor.
  • a stoichiometric chlorine oxyhydrogen flame is very particularly preferably used.
  • chlorine and hydrogen preferably diluted with inert gas, but in a stoichiometric ratio, on the surface of a porous carrier arranged in the reactor or provided with a catalytically active coating, which is provided with at least one feed line of chlorine and / or hydrogen , to be converted to hydrogen chloride.
  • the porous, catalytically active carrier can be a candle. It is also possible to use a support designed as a double tube, of which at least part of the wall or walls is porous. Sintered metal or ceramic can be used as the porous material. A metal can be used as the catalytically active component, which catalyzes the conversion of chlorine and hydrogen to hydrogen chloride, e.g. B. a platinum metal.
  • the conversion of chlorine and hydrogen to hydrogen chloride heats the gas stream to a sufficiently high temperature to initiate DCE pyrolysis.
  • the gas mixture can be adjusted so that
  • a reactor which has at least one catalytically active metal arranged on the inside on a gas-permeable support provided with a feed for flushing 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 metal.
  • Rhodium, ruthenium, palladium and platinum are very particularly preferred.
  • gas-permeable carrier which can be attached to selected areas of the inner wall of the reactor and / or the inside of the reactor and which are provided with feed lines for flushing gas.
  • This can be a cage, which is formed, for example, by a grid or a perforated metal plate, which can accommodate a catalyst bed and through which the flushing gas can flow, for example by central introduction by means of a perforated tube.
  • the gas-permeable support can be a gas-permeable plate which is surrounded by a flat structure, such as a wire mesh, made of catalytically active metal.
  • the gas-permeable carrier is preferably a porous one
  • Moldings This can consist of the catalytically active metal. It is preferably a porous ceramic which is coated in particular with the catalytically active metal; or it is a porous ceramic that is doped with the catalytically active metal.
  • the catalytically active metal can be attached in any form in or on the gas-permeable support. Such arrangements are known to the person skilled in the art.
  • the catalytically active metal can be in the form of moldings with the largest possible surface-to-volume ratio.
  • the catalytically active metal is preferably applied to the gas-permeable support as a coating and / or as a doping.
  • the gaseous reducing agent is fed in via the gas-permeable carrier connected to the feed for flushing gas and is fed through this to the catalytically active metal.
  • a catalytically active metal arranged on and / or in the gas-permeable carrier with a gaseous substance supplied through the gas-permeable carrier
  • Reducing agent preferably flushed with hydrogen or with a mixture of hydrogen and inert gas.
  • the gaseous reducing agent can be supplied 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 supplied via the gas-permeable carrier is expediently adapted to the temperature which prevails in the interior of the reactor at the location of the gas-permeable carrier.
  • Educt gas flow can increase sales in the pyrolysis reaction and increase the product yield;
  • the parallel rinsing with reducing agent allows the coking of the surface of the catalytically active metal, which may be attached to the inside of the reactor, to be efficiently prevented or slowed down, and thus the service life of the cracking furnace and the turnover of the
  • At least one feed line for a heated gas preferably opens in the vicinity of the entry of the feed gas stream into the reactor. This means that when the
  • Eduktgas formed in the reactor a high concentration of radicals, which contribute to an efficient course of the chain reaction.
  • the feed gas stream comes with several feed lines for a heated one as it passes through the reactor
  • the number of feed lines for a heated gas 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
  • 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 is continued using the heat supplied by the product gas stream while cooling the product gas, and in the interior of which at least one feed line for a heated gas optionally opens, and e) optionally introducing a heated gas through the feed line (s) opening into the adiabatic post-reactor , wherein the temperature of the heated gas is above the temperature of the product gas stream prevailing at the point of the feed line, and wherein the
  • the total amount of the heated gas added in the adiabatic post-reactor is not more than 10% by weight, based on the total mass flow in the adiabatic post-reactor.
  • the method according to the invention can only include measures d) and e) in the adiabatic post-reactor, without using an upstream reactor in whose interior at least one feed line for a heated gas opens.
  • the invention also relates to a reactor for carrying out the process defined above, comprising the elements: i) feed line for the educt gas stream containing saturated halogen-containing aliphatic hydrocarbon opening into the reactor, ii) at least one feed line for a heated gas opening into the interior of the reactor, iii) at least one heating device for heating the heated gas, which is attached directly in front of the reactor end of the feed line, iv) heating device for heating and / or maintaining the
  • 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) and iii) defined above.
  • the required heat of reaction is supplied by the heat of the product gas stream supplied, which cools down as a result.
  • Post-reactor can also be connected to a reactor known per se which does not have the elements ii) and iii).
  • the supply line for the heated gas preferably consists of metal pipelines which open into the reactor and which have a nozzle at their reactor-side end and which have an electrical heating device for the heated gas directly in front of their reactor-side end.
  • the feed line for the heated gas has a candle made of porous ceramic at its end on the reactor side, which is equipped on the inside with a heating device, for example with a heating cartridge.
  • At least one porous ceramic in the form of a candle is present inside the reactor, the surface of which is coated with catalytically active metal and / or which is doped with catalytically active metal, the candle is provided with a feed line for a equipped gaseous reducing agent for transmission to the catalytically active metal and the candle has an electric heating device for the heated gas.
  • Figure 1 A preferred device for heating and introducing the hot inert gas into a cracking reactor shown in longitudinal section
  • Figure 2 An arrangement of the device of Figure 1 in a reaction tube shown in longitudinal section
  • Figure 3 tubular reactor with device according to Figure 1 in longitudinal section
  • the feed gas stream comes with one or more as it passes through the reactor
  • the heating device is an electrically operated heating cartridge (1) which is attached directly in front of the reactor-side end of the feed line, which is preferably provided with a ceramic jacket and which is arranged in a housing (2) which has one or more concentric annular gaps (3).
  • the housing (2) can consist of ceramic and / or metal.
  • the housing preferably has a cylindrical shape.
  • the heating cartridge (1) is fixed in the housing (2) by means of a gastight, pressure and temperature resistant bushing (4).
  • This is preferably a bushing (4) provided with a screw thread, into which the heating cartridge can be screwed and fixed.
  • the housing (2) has a gas inlet (5) through which a gas stream consisting of an inert gas can be introduced via a feed line.
  • the gas inlet (5) is preferably located on the outer wall of the housing (2).
  • a plurality of concentric annular gaps (3) through which the inert gas flows are preferably formed in the housing.
  • These ring gaps (3) have at least two openings through which the inert gas flows into and out of the ring gap. These openings are preferably made at the level of the front and rear ends of the heating device. The consequence of this is that the inert gas flows through each annular gap along the entire length of the heating device and that the direction of flow of the inert gas reverses in each annular gap.
  • gas flow moves from the outside of the housing (2) through the ring gaps (3), is deflected several times in the ring gaps (3), and finally flows along the heating cartridge (1) fitted inside and then through a gas outlet ( 6), which is preferably designed as a nozzle, in the reaction chamber.
  • the housing (2) can also only have an annular gap. In this case, the gas immediately flows along the heating cartridge (1) through the gas outlet (6) into the reaction space.
  • FIG. 1 with a plurality of annular gaps offers the advantage that the outer wall of the heating device does not heat up or does not heat up significantly above the temperature prevailing in the reaction chamber due to the strong heating of the inert gas on the heating cartridge (1). This prevents the build-up of coke deposits on the outer wall.
  • the outer wall of the heating device in particular the part of the heating device which projects into the reaction space, can be coated with an inert material, e.g. B. a metal oxide, ceramic, boron nitride or silicon nitride.
  • an inert material e.g. B. a metal oxide, ceramic, boron nitride or silicon nitride.
  • the inner wall of the heating device opposite the heating cartridge (1) can be coated with such materials.
  • the heating device shown in Figure 1 is provided on its outer wall with a cone (8), on the outside of which there is a thread (7).
  • the cone (8) and that part of the heating device which forms the sealing edge for the line seal are made of materials which have approximately the same thermal expansion, in particular of the same material.
  • a possible arrangement of the heating device on the reaction tube is shown in Figure 2.
  • a holder (10) is welded to the reaction tube (9) and has a thread (11) and a projection (12) which forms a circumferential sealing edge.
  • the heating device shown in Figure 1 can be in a conventional
  • Tube 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.
  • such a furnace is fired with a primary energy source, such as with oil or gas, into a so-called radiation zone (16) and a convection zone
  • the heat required for the pyrolysis is transferred to the reaction tube primarily by radiation from the furnace walls heated by the burner.
  • the energy content of the hot flue gases emerging from the radiation zone is used by convective heat transfer.
  • the starting material of the pyrolysis reaction e.g. EDC
  • preheated 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 overheated there, the pyrolysis reaction already being able to start. After done Overheating, the EDC enters the radiation zone, where the conversion to vinyl chloride and hydrogen chloride takes place.
  • the cracking furnace is expanded by at least two additional, non-heated compartments (18) which can be thermally insulated. Loops of the reaction tube are then guided through these compartments (18) from the actual radiation or convection zone (16, 17). In these loops, preferably on the arches of the loops and ending in the horizontal sections of these loops, the heating device according to FIG. 1 (19) for introducing a heated inert gas is then mounted, that is to say built into the reaction tube, so that the educt gas flow coexists at these points can be brought into contact with the heated inert gas.
  • 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)
  • 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

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 au moins une conduite d'amenée de gaz haute température qui dépasse dans sa partie interne et par laquelle un gaz inerte de température supérieure à celle de l'éduit gazeux, est introduit en petite quantité dans le réacteur. Le procédé permet d'obtenir une augmentation du rendement en produit de la réaction de craquage.
PCT/EP2003/004506 2002-05-02 2003-04-30 Procede de preparation d'hydrocarbures halogenes insatures et dispositif utilise a cet effet WO2003093206A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AU2003233203A AU2003233203A1 (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
DE10219722.9 2002-05-02
DE2002119722 DE10219722B4 (de) 2002-05-02 2002-05-02 Verfahren zur Herstellung ungesättigter halogenhaltiger Kohlenwasserstoffe sowie dafür geeignete Vorrichtung
DE10307193.8 2003-02-20
DE2003107193 DE10307193A1 (de) 2003-02-20 2003-02-20 Verfahren zur Herstellung ungesättigter halogenhaltiger Kohlenwasserstoffe sowie dafür geeignete Vorrichtung

Publications (1)

Publication Number Publication Date
WO2003093206A1 true WO2003093206A1 (fr) 2003-11-13

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Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB736740A (en) * 1952-08-28 1955-09-14 Ici Australia Ltd Improvements in and relating to the dehydrochlorination of chlorinated hydrocarbons
GB938824A (en) * 1960-11-10 1963-10-09 Goodrich Co B F Preparation of vinyl chloride
US3641183A (en) * 1968-07-09 1972-02-08 Exxon Research Engineering Co Injection of an electrically heated stream into a steam cracked product
US3843744A (en) * 1972-02-14 1974-10-22 L Kramer Controlling coke in the pyrolysis of hydrocarbons to acetylene and hydrogen
US5488190A (en) * 1992-04-21 1996-01-30 Elf Atochem S.A. Prepartion of vinyl chloride by ultrapyrolysis of 1,2-dichloroethane
WO2002094743A2 (fr) * 2001-05-19 2002-11-28 Siemens Axiva Gmbh & Co. Kg Procede et dispositif pour realiser des reactions radicalaires en phase gazeuse

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB736740A (en) * 1952-08-28 1955-09-14 Ici Australia Ltd Improvements in and relating to the dehydrochlorination of chlorinated hydrocarbons
GB938824A (en) * 1960-11-10 1963-10-09 Goodrich Co B F Preparation of vinyl chloride
US3641183A (en) * 1968-07-09 1972-02-08 Exxon Research Engineering Co Injection of an electrically heated stream into a steam cracked product
US3843744A (en) * 1972-02-14 1974-10-22 L Kramer Controlling coke in the pyrolysis of hydrocarbons to acetylene and hydrogen
US5488190A (en) * 1992-04-21 1996-01-30 Elf Atochem S.A. Prepartion of vinyl chloride by ultrapyrolysis of 1,2-dichloroethane
WO2002094743A2 (fr) * 2001-05-19 2002-11-28 Siemens Axiva Gmbh & Co. Kg Procede et dispositif pour realiser des reactions radicalaires en phase gazeuse

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AU2003233203A8 (en) 2003-11-17

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