EP1784253A1 - Procede et dispositif pour la vaporisation de combustibles liquides - Google Patents

Procede et dispositif pour la vaporisation de combustibles liquides

Info

Publication number
EP1784253A1
EP1784253A1 EP05772809A EP05772809A EP1784253A1 EP 1784253 A1 EP1784253 A1 EP 1784253A1 EP 05772809 A EP05772809 A EP 05772809A EP 05772809 A EP05772809 A EP 05772809A EP 1784253 A1 EP1784253 A1 EP 1784253A1
Authority
EP
European Patent Office
Prior art keywords
reactor
liquid fuel
oxygen
containing gas
temperature
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP05772809A
Other languages
German (de)
English (en)
Inventor
Jochen Volkert
Ernst Keim
Conchita Encinas Bermudez
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.)
GVP Gesellschaft zur Vermarktung der Porenbrennertechnik mbH
Original Assignee
GVP Gesellschaft zur Vermarktung der Porenbrennertechnik mbH
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 GVP Gesellschaft zur Vermarktung der Porenbrennertechnik mbH filed Critical GVP Gesellschaft zur Vermarktung der Porenbrennertechnik mbH
Publication of EP1784253A1 publication Critical patent/EP1784253A1/fr
Withdrawn legal-status Critical Current

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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
    • B01J4/00—Feed or outlet devices; Feed or outlet control devices
    • B01J4/001—Feed or outlet devices as such, e.g. feeding tubes
    • B01J4/002—Nozzle-type elements
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01B—BOILING; BOILING APPARATUS ; EVAPORATION; EVAPORATION APPARATUS
    • B01B1/00—Boiling; Boiling apparatus for physical or chemical purposes ; Evaporation in general
    • B01B1/005—Evaporation for physical or chemical purposes; Evaporation apparatus therefor, e.g. evaporation of liquids for gas phase 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
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/0006—Controlling or regulating processes
    • B01J19/0013—Controlling the temperature of the process
    • 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
    • B01J8/0242—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 vertical
    • B01J8/025—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 vertical in a cylindrical 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
    • 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
    • B01J8/0278—Feeding reactive fluids
    • 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
    • B01J8/0285—Heating or 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
    • B01J8/02—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
    • B01J8/0292—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 with stationary packing material in the bed, e.g. bricks, wire rings, baffles
    • 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; Reversible storage of hydrogen
    • C01B3/02—Production of hydrogen; Production of gaseous mixtures containing hydrogen
    • C01B3/32—Production of hydrogen; Production of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide or air
    • C01B3/34—Production of hydrogen; Production of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide or air by reaction of hydrocarbons with gasifying agents
    • C01B3/36—Production of hydrogen; Production of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide or air by reaction of hydrocarbons with gasifying agents using oxygen; using mixtures containing oxygen as gasifying agents
    • 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
    • B01J2208/00026—Controlling or regulating the heat exchange system
    • B01J2208/00035—Controlling or regulating the heat exchange system involving measured parameters
    • B01J2208/00044—Temperature measurement
    • B01J2208/00061—Temperature measurement of the reactants
    • 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
    • B01J2208/00389—Controlling the temperature using electric heating or cooling elements
    • B01J2208/00398—Controlling the temperature using electric heating or cooling elements inside the reactor 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
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00051—Controlling the temperature
    • B01J2219/00054—Controlling or regulating the heat exchange system
    • B01J2219/00056—Controlling or regulating the heat exchange system involving measured parameters
    • B01J2219/00058—Temperature measurement
    • B01J2219/00063—Temperature measurement of the reactants
    • 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
    • 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
    • C01B2203/025—Processes for making hydrogen or synthesis gas containing a partial oxidation 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
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
    • C01B2203/085—Methods of heating the process for making hydrogen or synthesis gas by electric heating
    • 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
    • C01B2203/12—Feeding the process for making hydrogen or synthesis gas
    • C01B2203/1205—Composition of the feed
    • C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
    • C01B2203/1235—Hydrocarbons
    • C01B2203/1247—Higher hydrocarbons
    • 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
    • C01B2203/12—Feeding the process for making hydrogen or synthesis gas
    • C01B2203/1276—Mixing of different feed components
    • 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
    • C01B2203/12—Feeding the process for making hydrogen or synthesis gas
    • C01B2203/1288—Evaporation of one or more of the different feed components
    • 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
    • C01B2203/16—Controlling the process
    • C01B2203/1604—Starting up the process

Definitions

  • the invention relates to a method and a device for the evaporation of liquid fuel.
  • WO 00/06948 discloses a method for evaporating liquid fuel according to the "cold flame principle".
  • the “principle of the cold flame” is meant a partially exothermic oxidation of hydrocarbons at atmospheric pressure at a temperature in the range of 300 to 500 ° C. In this exothermic reaction about 10 to 15% of the stored chemical energy is released. The reaction according to the "principle of the cold flame” does not lead to the formation of a visible flame.
  • the object of the invention is to eliminate the disadvantages of the prior art.
  • a method and a device are to be specified with which a vaporization and exothermic reaction according to the principle of the cold flame can be carried out in as simple, safe and cost-effective manner as possible.
  • the device should also make it possible to carry out the "partial oxidation" process.
  • a method for the evaporation of liquid fuel is provided with the following steps:
  • a “reactor” is understood to mean a container which encloses a free volume. It may be, for example, a cylindrical tube.
  • a means for increasing the internal surface is included in the reactor.
  • the inventively provided means for increasing the inner surface contributes to an increase in the effective heat conductivity and / or the volumetric heat exchange coefficient in the reactor. As a result, a reactor surrounded and heated to a predetermined temperature
  • the exothermic reaction of the present invention is a reaction that proceeds without ignition and formation of a visible, open flame.
  • the liquid fuel is only partially oxidized. It may be that a pre-reacted mixture is already fed to the reactor or a partially reacted mixture is removed from the reactor.
  • suitable means for producing a prereacted mixture or for continuing the reaction of a partially reacted mixture may be upstream or downstream of the reactor.
  • the heat generated in the exothermic reaction is z. T. transferred to the reactor. This is u.a. as a heat storage. In a suitable process procedure, it is only necessary to start the exothermic reaction.
  • the exothermic reaction may be an exothermic reaction according to the "principle of the cold flame".
  • the temperature in the reactor is so regulated that a lower temperature limit of 22O 0 C is not undershot and an upper temperature limit of 600 0 C is not exceeded.
  • the air ratio ⁇ of a mixture formed from the liquid fuel and the oxygen-containing gas can assume any desired values.
  • the air ratio ⁇ is the ratio between the actual amount of air and the amount of air theoretically required for complete combustion.
  • an exothermic reaction according to the "cold flame principle" can be carried out continuously.
  • the temperature is suitably regulated in the reactor, that a lower temperature limit of 600 0 C range and an upper temperature limit of 1500 0 C is not exceeded.
  • the air ratio ⁇ of a mixture formed from the liquid fuel and the oxygen-containing gas is ⁇ 1.
  • the two aforementioned alternative variants of the method can advantageously be carried out in one and the same device.
  • the aforementioned temperature ranges apply to atmospheric pressure.
  • the indicated temperature window is to be adapted accordingly.
  • the liquid fuel is at most to
  • the liquid fuel is atomized on entering the reactor.
  • the reactor may have a mixing section upstream, in which one from the. atomized liquid fuel and the oxygen-containing gas formed mixture is produced.
  • means for fluid mechanical stabilization can be included in the mixing section. These may be flow baffles and the like. This ensures that a homogeneous Gemischbil ⁇ tion is guaranteed in the mixing section in a large modulation range. The mixture is always generated and homogenized by the proposed means for stabilizing the flow in the mixing section.
  • the means taken in the reactor to increase the inner surface also serves to keep the reaction zones in the reactor over a wide modulation range away relative to the axial extent of the reactor in a predetermined area. Thus, an evaporation product with given properties can always be produced across the entire modulation range.
  • an air nozzle for introducing the air into the mixing section can be provided with a swirl generator as a means for stabilizing the flow. It can thus be generated with a twisted or untwisted free jet. Further, an exit diameter of the air nozzle and a distance of the air nozzle to the means for increasing the inner surface can be varied.
  • the free jet causes recirculation of the energy and the chemical radicals within the mixing section.
  • the means for increasing the inner surface thus causes a determination of certain reaction zones within the reactor. The boundaries of the reaction zones depend on the power with which the device is operated. Depending on the modulation range, they vary within a given axial range. However, the means for increasing the internal surface ensures that the reactor Onszonen as such over the entire modulation range er ⁇ hold and thus always the given Verdampfungs ⁇ product is generated.
  • Preheating the reactor serves to start and / or maintain the exothermic reaction.
  • the reactor can be preheated, for example, by combustion of a mixture formed from the liquid fuel and the oxygen-containing oxidant. In this case, the mixture is adjusted so that combustion can take place.
  • combustion is stopped.
  • a mixture of liquid fuel and oxygen-containing gas without the formation of a visible flame in the reactor exo ⁇ therm partially oxidized and thus evaporated.
  • the heat released in the exothermic reaction expediently heats the means for increasing the inner surface.
  • the reactor is heated with an electric heating element.
  • a heating element is used in particular for starting the reactor to start the exothermic reaction. If, during operation of the reactor, excessive cooling of the reactor occurs, then heat can be supplied again by means of the electrical heating element.
  • hot exhaust gases can also be recirculated, which are formed, for example, by combustion of the product.
  • a chamber can be provided downstream of the reactor, from which a recirculation line branches off to recirculate the product.
  • the reactor can also be a burner with a
  • Downstream combustion chamber from which a recirculation line for recirculation of hot exhaust gases branches off.
  • Recirculation lines can be connected, for example, to the above-mentioned mixing section.
  • the oxygen-containing gas can also be heated indirectly via a heat exchanger, which is heated with the hot exhaust gases or the hot product.
  • the means for increasing the inner surface is used as the heating element.
  • the means for increasing the inner surface is expediently designed as a resistance heating element.
  • it may be made of metal, silicon carbide or the like.
  • Such gas can be a waste product of another process.
  • the temperature of the reactor can be conveniently controlled by increasing or decreasing the temperature of the oxygen-containing gas supplied. It is also possible to control the temperature of the reactor by increasing or decreasing the mass flow of the oxygen-containing gas through the reactor. In these cases u. U. be dispensed with a heating element for heating the reactor.
  • Air can be used as the oxygen-containing gas and hydrocarbons as the liquid fuel, preferably light heating oil or diesel.
  • any oxygen-containing gas in conjunction with all oxidizable hydrocarbon-containing fuels is suitable for carrying out the exothermic reaction according to the "cold flame” principle and / or the "partial oxidation".
  • the means for increasing the inner surface is expediently a permeable, porous medium and can be selected from the following group: Porous bodies, eg. For example, with a foam structure made of ceramic or metal, static shear, wire or Fasergewirk, tube assembly, bed, arrangement of perforated plates.
  • Porous bodies eg.
  • a foam structure made of ceramic or metal, static shear, wire or Fasergewirk, tube assembly, bed, arrangement of perforated plates.
  • the means for increasing the inner surface of a ceramic, a glass, a binder or made of metal is an agent which is temperature resistant. It may be that the means for increasing the inner surface is provided with a catalytic coating.
  • the means for increasing the inner surface is expediently received in a cylindrical reactor housing. It is in any case designed such that a flow through the reactor from an inlet to an outlet is possible and at the same time the heat released during the exothermic reaction is stored in an effective manner by the means for increasing the internal surface for its further maintenance.
  • a device for the evaporation of liquid fuel with a Reak ⁇ tor, in which a means for increasing the inner surface is added, a means for supplying wellssigbrenn ⁇ material and oxygen-containing gas in the reactor, and a Means for controlling the temperature of the reactor such that an exothermic reaction between the oxygen-containing gas and the evaporating liquid fuel is feasible such that the liquid fuel is only partially oxidized.
  • the proposed device is simple and inexpensive to produce.
  • By carrying out the reaction in a reactor in which a means for increasing the internal surface area is provided it is possible to more safely and reliably avoid undesired ignition of the mixture while forming a free, visible flame in the reactor.
  • the temperature in the reactor can be regulated with the means for controlling so that a lower temperature limit of 220 ° C. is not undershot and an upper temperature limit of 1500 ° C. is not exceeded.
  • the temperature in the reactor on the one hand, can be kept constant, for example in a temperature range from 22O 0 C to 600 0 C, so that in this temperature range an exothermic reaction according to the principle of the "cold flame" can be carried out.
  • the performance of the device can be modulated in a wide range.
  • the control it is possible to operate the device either in accordance with the principle of the "cold flame” in a first temperature range or according to the principle of "partial oxidation” in a second temperature range.
  • only a single structural design of the device is necessary. It is suitable for carrying out both of the above-mentioned process variants.
  • a means for atomizing the remplissig ⁇ fuel is provided.
  • a particularly homogeneous mixture can be produced.
  • the vaporized product made therefrom is also particularly homogeneous.
  • the sputtering means may comprise at least one nozzle.
  • the nozzle in turn may be surrounded by an annular nozzle for supplying oxygen-containing gas.
  • the annular nozzle is provided with a swirling element.
  • the oxygen-containing gas can be added, for example, in a rotating about the axis of the annular nozzle flow.
  • the annular nozzle and possibly the swirling element can open in a mixing section of the reactor, which upstream the means for increasing the inner surface is arranged.
  • a homogeneous mixture of the oxygen-containing gas and the finely atomized liquid fuel is formed.
  • an ignition device for igniting the mixture can be provided. By Ver ⁇ combustion of the mixture, a preheating of the device can be achieved in a simple manner.
  • a means for supplying hot gases to the reactor is provided. This may be the product discharged from the reactor or also exhaust gases from a downstream combustion process or other hot exhaust gases.
  • a device for injecting the liquid fuel may be provided under a pressure in the range of 3 to 100 bar.
  • a variation of the pressure allows operation of the device with a predetermined power.
  • a means for injecting the liquid fuel is provided at a predetermined clock frequency.
  • the agent may be fast closing valves. Such valves can be operated with a frequency in the range of 5 to 70 Hz. The amount of liquid fuel to be injected can be controlled by the closing time of such valves.
  • an electrical heating element is provided for heating the reactor. It may be a heating coil or the like surrounding the reactor. Furthermore, a means for heating the supplied oxygen-containing gas can be provided. The means for supplying may further comprise a fan for supplying the oxygen-containing gas into the reactor. The means for heating the supplied oxygen-containing gas can spielmik be integrated into the blower and also from Heating coils exist, through which the oxygen-containing gas is passed.
  • the heating element is expediently accommodated in the annular nozzle or in a space upstream of the ring nozzle, preferably an annular space.
  • the annular nozzle at least partially pass through the room.
  • the nozzle can be surrounded at least in sections by a thermal shielding device in a section which passes through the space. It may be, for example, one or more protective tubes.
  • a reactor housing is part of a heat exchanger, through which the oxygen-containing gas is fed to the reactor zu ⁇ .
  • This makes it possible in a simple and cost-effective manner to preheat the supplied oxygen-containing gas through the heat released in the reactor during combustion according to the "cold flame" principle.
  • This allows an autothermal operation of the device, in particular, no energy must be supplied to heat the reactor.
  • the reactor can be operated in a wide power dynamic range.
  • the oxygen-containing gas can be preheated with the heat exchanger to a temperature of up to 300 ° C. The preheating advantageously causes avoidance of condensation.
  • the heat exchanger expediently has a first annular channel formed between a first inner housing and the reactor housing, through which the oxygen-containing gas is passed.
  • the circulation of the reactor with the oxygen-containing gas avoids unwanted cooling of the reactor by the emission of heat.
  • the first ring channel may be connected to the ring nozzle.
  • a second annular gap for discharging a thilde formed in the reactor the partially vaporized liquid fuel containing Product be provided.
  • At least one sensor is provided for measuring the temperature prevailing in the reactor. It may be a conventional thermocouple. Of course, it is also possible to provide several sensors for measuring the temperature along the flow path. This makes possible a refined control of the temperature prevailing in the reactor and / or the setting of a given temperature profile along the flow path in the reactor.
  • the means for regulating the temperature as a function of the temperature measured by the sensor on the basis of a predetermined algorithm controls the power of the electric heating element and / or the means for heating the supplied oxygen-containing gas and / or of the blower.
  • the means for regulating the temperature may include a conventional control with a microprocessor which effects the regulation of the temperature according to a predetermined control algorithm.
  • the means for increasing the inner surface is expediently produced from one of the following materials: ceramic, glass, binder, metal.
  • the agent for increasing the inner surface may be selected from the following group: Porous bodies, eg. B. foam or
  • FIG. 1 is a schematic view of a device according to the invention
  • FIG. 2 shows the pore body according to FIG. 1 and the temperature profile prevailing in the pore body during the exothermic reaction
  • FIG. 5 is a cross-sectional view according to the section line A- A 'in Fig. 4,
  • FIG. 9 is a side view of the heating element of FIG. 8,
  • FIG. 12 is an enlarged partial sectional view of FIG. 11,
  • FIG. 13 is a sectional view of a first heater
  • FIG. 14 is a plan view of FIG. 13,
  • 15 is a sectional view of a sixth reactor, 16 is an enlarged partial sectional view of FIG. 15,
  • 17 is a sectional view of a second heater
  • FIG. 17 is a side view of FIG. 17,
  • FIG. 19 is a plan view of FIG. 17,
  • 21 is a schematic view of another device according to the invention.
  • Fig. 22 is a partial sectional view of the seventh reactor with a first ignition device received therein and
  • Fig. 23 is a partial sectional view of the seventh reactor with a second igniter received therein.
  • a porous body 1 is shown, which is made of, for example, a porous ceramic, a porous metal, a Draht ⁇ braid or the like.
  • the porous body 1 has a communicating pore space, so that a mixture consisting of air L and vaporized or partially vaporized liquid fuel 0 can flow through.
  • the porous body 1 can be made cylindrical and accommodated in a correspondingly designed housing or reactor (not shown here).
  • the reactor can conventionally have in each case an inlet for the air L and the liquid fuel O or else a common inlet for a premixture formed from the air L and the liquid fuel O.
  • the reactor For discharging the product formed in the porous body 1, the reactor has an outlet in a conventional manner (not shown here).
  • a blower 2 is provided, which is provided with a heater 3. 4 designates a pump with which liquid fuel O can be sprayed in an atomized form through the nozzle provided thereon (not shown here) into the free volume in front of the pore body 1.
  • the air L can by a suitably designed feeder, z. B. by means of an air nozzle, are guided in the free volume such that forms a free jet.
  • a suitably designed feeder z. B. by means of an air nozzle
  • the fuel is supplied in the vicinity of the axis of the free jet by atomizing the flüssi ⁇ gen fuel by means of a centrally disposed nozzle, whereby a very large surface area of the fuel is generated and intensive mixing of the fuel with the air L takes place.
  • the upstream free volume were ⁇ caused by the free jet recirculation flows whose size u. a.
  • a heating element 5, shown schematically here, can surround the pore body 1.
  • the heating element 5 can also surround the reactor. It may also be that the means for increasing the inner surface itself is designed as a resistance heating element.
  • the porous body 1 is further provided with a thermocouple 6 for measuring the temperature prevailing therein.
  • the thermoelement 6 is connected to a control unit 7.
  • the control unit 7 serves to control the temperature of the pore body 1.
  • the control unit 7 can do this with the blower 2, the Heating device 3, the pump 4 and the heating element 5 ver ⁇ be connected.
  • one or more of the aforementioned components for controlling the temperature can be controlled ge according to a predetermined algorithm, so that the temperature of the pore body 1, for example, in a range from 360 to 400 ° C is kept constant.
  • the temperature of the porous body 1 can be influenced by the temperature of the supplied air L, which is adjustable by means of the heating device 3.
  • FIG. 2 again shows the pore body 1 shown in FIG. 1 and an example of a temperature profile formed along this pore body 1 during the execution of the exothermic reaction.
  • FIG. 3 shows a reactor 8 produced, for example, from a metal or ceramic tube, in which the porous body 1 is accommodated.
  • a mixing section 9 Upstream of the porous body 1 is a mixing section 9, in which an air nozzle 10 and a liquid fuel nozzle 11 open.
  • a distance of an outlet cross-section of the air nozzle 10 to the downstream downstream porous body 1 is denoted by S and a Austritts ⁇ cross-section of the air nozzle 10 with d.
  • the air nozzle 10 and the liquid fuel nozzle 11 also two-fluid nozzles and the like. Can be used.
  • a temperature increase over the axial extent of the reactor 8 is determined, but the gradient of the temperature rise is markedly reduced after entry into the pore body 1.
  • the porous body 1 causes temperature deviations to be maintained transversely to the flow direction within a relatively narrow range.
  • the maximum temperature is limited at the position indicated as cold flame oxidation of kohlenwasserstoffhal- term fuels to about 500 0 C.
  • the product formed in the exothermic reaction, z. As a consisting of air L and liquid fuel O steam and product gases is discharged at the exit of the pore body 1.
  • a homogeneous temperature distribution predominates over the entire volume of the pore body 1, essentially.
  • the exothermic reaction according to the "principle of the cold flame” or the "partial oxidation” can be performed particularly homogeneous.
  • the product leaving the porous body 1 has hardly any concentration fluctuations.
  • the pore body 1 acts like a heating element 5, which generates a constant reaction temperature in the entire reaction volume. Local overheating or undesired cooling in the reaction volume is avoided by the use of the porous body 1 proposed according to the invention.
  • a reactor housing 12 preferably cylindrical in shape, is provided with an inlet 12a for supplying air L.
  • a first annular gap 14 is formed between a first inner housing 13 received therein and the reactor housing 12.
  • the inner housing has a baffle plate 12b opposite the inlet 12a, at which the air L supplied through the inlet 12a is deflected and guided in the first annular gap 14.
  • the first annular gap 14 connects the inlet 12a with an annular space 15 surrounding the liquid fuel nozzle 11.
  • the annular space 15 is connected to the mixing section 9 via the air nozzle 10.
  • the mixing section 9 and the pore body 1 provided downstream are accommodated in a second inner housing 16, which is surrounded by the first inner housing 13 with the formation of a second annular gap 17.
  • the first inner housing 13 and the second inner housing 16 may be cylindrical as well as the reactor housing 12 and arranged coaxially.
  • the open to the porous body 1 second annular gap 17 opens through the annular space 15 sweeping transfer channels (not shown here) in a plenum 18 and from there into an outlet 19th
  • the reference numeral 20 denotes a protective tube which shields the liquid fuel nozzle 11 against thermal influences.
  • FIG. 5 shows a schematic sectional view according to the section line A-A 'in FIG. 4.
  • the overflow channels 21 penetrating the annular space 15 and a swirl generator 22 arranged in the air nozzle 10 can be seen here.
  • Fig. 6 shows a sectional view through a third reactor.
  • the third reactor differs from the second reactor in particular in that the protective tube 20 extends to the mouth of the air nozzle 10.
  • the protective tube 20 extends to the mouth of the air nozzle 10.
  • the heating elements 5 can each extend within the annular space 15 either parallel to its longitudinal axis to the longitudinal axis of the liquid fuel nozzle 11 or also perpendicular thereto.
  • a resistance wire 23 may be wound separately by an insulation 24 in the manner of a helix on a ceramic rod 25.
  • Reference numeral 26 designates electrical connections which correspond to the resistance standing wire 23, which may for example consist of ISA chrome 60, are connected.
  • Fig. 10 shows a possible arrangement of the in Figs. 8 and.
  • the heating elements 5 are arranged with their axis perpendicular to the axis of the liquid fuel nozzle 11 and project into the annular space 15. They can surround the liquid fuel nozzle 11 in a star shape, so that the air L preheated by the annulus 15 and then through the Air nozzle 10 is ejected.
  • heating elements 5 designed in the manner of a heating coil are arranged in a third annular gap 27, which connects the annular space 15 to the air nozzle 10.
  • a multiplicity of heating elements 5 are provided which surround the protective tube 20 radially in the third annular gap 27.
  • a thermal insulation 28 may be included in a rear space bounding the annulus 15.
  • Figs. 15 to 19 show a sixth reactor.
  • the heating elements 5, which in turn are designed in the form of a helix, are arranged with their axes parallel to the liquid fuel nozzle 11.
  • a carrier element 29 accommodating the heating elements 5 is designed such that it extends over the entire length of the annular space 15.
  • the guided through the annular space 15 air L is preferably guided by the heating elements 5 to the air nozzle 10 necessarily.
  • cooling air L1 can be passed through a further inlet 30 into the protective tube 20 for additional cooling of the liquid fuel nozzle 11.
  • a thermal shielding device 31 for example a further protective tube, which surrounds the protective tube 20 may be provided in the annular space 15.
  • Fig. 21 shows schematically a device with a seventh reactor. In this case, downstream of the blower 2, an adjusting element 32 downstream of which the proportion of air L supplied to the inlet 12a and the proportion of cooling air L1 fed to the further inlet 30 can be adjusted.
  • an ignition device 33 projects into the mixing section 9 in each case. It can be a device for generating a spark (see FIG. 22) or else an ignition device Glü ⁇ h sensible (see Fig. 23) act.
  • Air L supplied by the blower 2 passes through the first annular gap 14 into the annular space 15.
  • the air L is preheated by the hot product discharged from the reactor 8 in the second annular gap 17.
  • a circulating air flow is generated by means of the swirl generator 22, with which the air L exits the air nozzle 10.
  • the air L mixes with finely atomized liquid fuel emerging from the liquid fuel nozzle 11, for example light oil.
  • the homogeneous mixture produced enters the porous body 1, which is located on a suitable for carrying out the reaction according to the principle of "kal ⁇ tem flame” temperature. It comes in particular in the pore body 1 to the reaction according to the principle of the "cold flame”.
  • the hot, partially oxidized product formed is deflected at the baffle plate 12b by approximately 140 degrees and exits the reactor 8 in the opposite flow direction through the second annular gap 17, the overflow channels 21 and the outlet 19.
  • the mixing chamber 9 preheated and / or kept at a suitable Tem ⁇ temperature.
  • the product emerging from the pore body 1 is therefore used both to maintain a suitable temperature in the mixing section 9 and to preheat the air L supplied through the first annular gap 14.
  • the baffle plate 12b may be made of a thermally insulating material. Depending on the thermal insulation capacity of the baffle plate 12b, it is thus possible to set a temperature in the reactor 8 or to stabilize a temperature distribution in the device. A further stabilization of the temperature conditions can be achieved by a suitable choice of the ratio between length and diameter of the reactor.
  • the heating elements 5 shown in FIGS. 7 to 19 can be used.
  • the proposed method and the device are easy to handle. They are available at low cost.
  • the proposed device can be used with conventional components, eg. As burners, chemical plants, engines and the like. Combine readily.
  • the device can be operated not only in the aforementioned mode of operation according to the principle of the "cold flame", but also in the further mode of operation of the "partial oxidation". For this it is only necessary to adjust the tempera- in the reactor 8 in a range of 600 to 1500 0 C to rule.
  • the "partial oxidation” reaction is different from the “cold flame” reaction.
  • the “partial oxidation” involves oxidation reactions with complete decomposition of the CH chains to produce hydrogen (H 2 ) and carbon monoxide (CO).
  • the reaction according to the "cold flame” principle only leads to a disintegration of the long CH chains.
  • the inventively proposed device can be operated without kon ⁇ structural change in both modes. For a particularly high modulation of the performance of the device is possible.
  • the device according to the invention is particularly suitable for operating burners with a high power modulation.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Physics & Mathematics (AREA)
  • Fluid Mechanics (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Inorganic Chemistry (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)

Abstract

L'invention concerne un procédé servant à vaporiser un combustible liquide (O) et comprenant les étapes suivantes : a) mise à disposition d'un réacteur (8) dans lequel est placé un moyen (1) servant à augmenter la surface intérieure ; b) amenée de combustible liquide (O) et de gaz oxygéné (L) dans le réacteur (8) ; c) exécution d'une réaction exothermique entre le gaz oxygéné (L) et le combustible liquide vaporisé (O), le combustible liquide (O) n'étant que partiellement oxydé ; d) extraction du réacteur (8) du produit formé lors de la réaction exothermique.
EP05772809A 2004-08-30 2005-08-20 Procede et dispositif pour la vaporisation de combustibles liquides Withdrawn EP1784253A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE200410041815 DE102004041815A1 (de) 2004-08-30 2004-08-30 Verfahren und Vorrichtung zur Verdampfung von Flüssigbrennstoffen
PCT/EP2005/009016 WO2006024410A1 (fr) 2004-08-30 2005-08-20 Procede et dispositif pour la vaporisation de combustibles liquides

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EP1784253A1 true EP1784253A1 (fr) 2007-05-16

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WO (1) WO2006024410A1 (fr)

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US20070113476A1 (en) * 2005-11-21 2007-05-24 Thomas Stephen M Fuel reformer and method of using the same
DE102006016912A1 (de) * 2006-04-11 2007-12-13 Forschungszentrum Jülich GmbH Verfahren zum Verdampfen eines flüssigen Kraftstoffs sowie eine Mischkammer zur Durchführung dieses Verfahrens
DE102006024038A1 (de) * 2006-05-23 2007-11-29 Forschungszentrum Jülich GmbH Vorrichtung zur Herstellung eines Kraftstoff-Oxidationsmittel-Gemisches
DE102006039933A1 (de) * 2006-08-25 2008-02-28 Enerday Gmbh Reformer zum Umsetzen von gasförmigem Brennstoff und Oxidationsmittel zu Reformat
DE102006043128A1 (de) * 2006-09-14 2008-03-27 Enerday Gmbh Reformer
DE102007017787A1 (de) * 2007-04-16 2008-10-30 Enerday Gmbh Reformer mit einer Katalysatoreinrichtung und einem Wärmeübertrager sowie Verfahren zum Betreiben eines Reformers
EP2168911A1 (fr) * 2008-09-30 2010-03-31 D. Kanbier Oxydation partielle d'hydrocarbures dans des conditions de flamme légères
DE102009026808A1 (de) * 2009-06-08 2010-12-09 aDROP Feuchtemeßtechnik GmbH Vorrichtung zum Verdampfen von Flüssigkeiten
DE102009039276A1 (de) 2009-08-28 2011-03-10 Bekon Energy Technologies Gmbh & Co. Kg Reaktormodul für endotherme Reaktionen sowie Reaktor mit einer Mehrzahl von solchen Reaktormodulen
DE102011113699A1 (de) 2011-09-20 2013-03-21 Lurgi Gmbh Verfahren zur Herstellung von Synthesegas
AT517361B1 (de) * 2015-06-30 2017-01-15 Avl List Gmbh Vorrichtung und Verfahren zum Entfernen von flüchtigen Partikeln aus einem Probengas
DE102018005694A1 (de) * 2018-07-19 2020-01-23 Linde Aktiengesellschaft Stoff- und/oder Wärmeaustauschkolonne und Verfahren zur Behandlung eines ersten Fluids und eines zweiten Fluids unter Verwendung einer Stoff- und/oder Wärmeaustauschkolonne
EP3650753B1 (fr) * 2018-11-12 2022-11-09 WS Wärmeprozesstechnik GmbH Procédé et dispositif de combustion étagée sans inflammation

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EP1102949B1 (fr) * 1998-07-29 2002-10-09 Heinrich Köhne Procede de valorisation d'un combustible par recours a des prereactions exothermiques sous forme de flamme froide
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CA2449205C (fr) * 2001-06-02 2010-05-18 Gvp Gesellschaft Zur Vermarktung Der Porenbrennertechnik Mbh Procede et dispositif pour la combustion non catalytique peu polluante d'un combustible liquide
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DE102004041815A1 (de) 2006-03-09

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