EP2928991A1 - Dispositif et procédé de craquage de gaz - Google Patents

Dispositif et procédé de craquage de gaz

Info

Publication number
EP2928991A1
EP2928991A1 EP13805823.5A EP13805823A EP2928991A1 EP 2928991 A1 EP2928991 A1 EP 2928991A1 EP 13805823 A EP13805823 A EP 13805823A EP 2928991 A1 EP2928991 A1 EP 2928991A1
Authority
EP
European Patent Office
Prior art keywords
gas
bed
combustion chamber
heat exchanger
reactor
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP13805823.5A
Other languages
German (de)
English (en)
Inventor
Dragan Stevanovic
Thomas OEHMICHEN
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.)
Krones AG
Original Assignee
Krones AG
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 Krones AG filed Critical Krones AG
Publication of EP2928991A1 publication Critical patent/EP2928991A1/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • 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
    • B01J8/04—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 passing successively through two or more beds
    • B01J8/0496—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
    • 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
    • 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
    • B01J8/04—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 passing successively through two or more beds
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/36—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using oxygen or 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
    • B01J2208/00106—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
    • 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
    • B01J2208/02—Processes carried out in the presence of solid particles; Reactors therefor with stationary particles
    • B01J2208/023—Details
    • B01J2208/027—Beds
    • 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
    • C01B2203/0255—Processes for making hydrogen or synthesis gas containing a partial oxidation step containing a non-catalytic 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
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0435—Catalytic purification
    • 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
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • 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
    • C01B2203/14—Details of the flowsheet
    • C01B2203/142—At least two reforming, decomposition or partial oxidation steps in series

Definitions

  • the present invention relates to an apparatus and a method for cracking gases, in particular gases from gasification processes of carbonaceous starting materials.
  • a device for cracking gases with a feed line for a carbonaceous gas by means of which the gas of a first bed of a thermal storage mass zuleitbar, a downstream in the flow direction of the gas disposed first combustion chamber having a controllable supply means for another, oxygen-containing gas , by means of which by substoichiometric oxygen supply partial oxidation of the carbonaceous gas takes place, and a subsequently arranged in the flow direction of the gas of the first combustion chamber reactor having a bed of a catalytically active material for the catalytic cracking of impurities of the carbonaceous gas provided.
  • Gases in particular gases from gasification processes of carbonaceous starting materials, may be contaminated with substances which may not oppose an energetic use of the gas depending on the type of contamination, but prevent further material use of these gases for the production of eg methanol, diesel or gasoline. But even with an energetic use of these gases, the removal of these impurities may be necessary, for example, to prevent damage and / or deposits in a turbine or piston engine. Depending on the type of use, it may therefore be necessary to remove these impurities from the gases. Especially in the material use is very high demands on the Gas quality, since otherwise significantly reduce the service life of the catalysts used for the chemical conversion.
  • impurities such as NH 3 , HCN, H 2 S, COS, halogens, alkalis, tars and others and dusts may be present, especially the mentioned tars in the removal are significant.
  • thermo-chemical gasification of carbonaceous feedstocks e.g. Biomass, coal or plastic waste to understand.
  • tars are understood to be complex multicomponent mixtures of organic components, in particular cyclic and polycyclic aromatic hydrocarbons.
  • the loading of a gas obtained by a gasification process with tars may, in addition to the carbonaceous starting material, for example, also be dependent on the gasification conditions and the type of gasifier.
  • the tar content in the gas stream may for example be between 1 and 100 g / m 3 .
  • Measures for tar reduction in gases are already known from the prior art. These can basically be subdivided into primary and secondary measures. Primary measures are understood to mean techniques that are already used during the gasification process. Secondary measures are arranged downstream or downstream of the gasifier. The latter can be divided into two main categories: physical processes and cracking / reforming.
  • Physical gas cleaning measures include electrostatic precipitators, cyclones, filters, and water and oil based scrubbers. These methods have the disadvantage that a subsequent energetic and material recycling is not readily possible.
  • thermal cracking In cracking / reforming, a distinction is made between thermal cracking and catalytic cracking / reforming.
  • thermal cracking For purely thermal cracking, cracking without Presence of a catalytically active substance, temperatures of at least 1000 ° C are necessary. For complete conversion of eg naphthalene even temperatures greater than 1400 ° C are necessary.
  • the associated high energy demand is often associated with a loss of calorific value.
  • the formation of undesirable by-products in the form of solid carbon deposits during thermal cracking can be significantly increased.
  • catalytic tar removal the tar is reacted on a catalytically active substance at temperatures of, for example, 800 to 900 ° C.
  • catalysts for example natural minerals such as dolomite or olivines or synthetic catalysts such as Ni-steam reforming catalysts can be used. However, the latter do not have sufficient life due to deactivation by sulfur and / or high tar loadings.
  • a disadvantage of all cracking / reforming processes is the energy required to achieve the high reaction temperatures.
  • the patent DE 195 21 673 describes a method for regenerative exhaust air purification, are used in the two large and a small storage mass to heat the exhaust air before the pollutants are burned and cool again after combustion, in a next step, the waste heat for heating to use. This should also achieve higher energy efficiency.
  • the document WO 02/051965 describes a cracking process in a fixed bed reactor with reverse flow.
  • a gas to be cracked is passed through a bed in a combustion chamber in which the temperature is maintained by adding oxygen.
  • the gas is then discharged via a second bed of the combustion chamber. Due to the heat stored in the fixed bed and the periodic flow reversal, a high heat recovery is possible.
  • a third bed is also used for flushing.
  • a disadvantage of the presented in the document WO 02/051965 method proves insufficient at low temperatures selectivity to the desired cracking products, which manifests itself in a much higher tendency to form solid carbon deposits. This is especially important when heating the gas.
  • the coking rate depends on a variety of parameters such as bulk material, tar composition and concentration, gas composition, temperature and residence time.
  • the formation of coke leads in the long term to an increase in the pressure loss over the bed.
  • dusts contained in the gas can deposit on the bed, so that it can lead to an additional pressure loss here.
  • the use of catalytic materials as a storage material is limited, as they often have to be used in a defined temperature window. Due to the temperature gradient in the bed only small volumes and low residence times are therefore possible.
  • the present invention has for its object to provide an apparatus and a method for the utilization of hydrocarbons available, which allow high efficiency and high efficiency. Furthermore, it is an object to further minimize the energy expenditure and the heat losses for cracking or reforming processes, as well as to improve the gas quality for subsequent processes. It is a further object to minimize the undesirable formation of tar by-products and to provide the ability to place a catalytically active substance in sufficient volume at an optimum reaction temperature within a gas cracking apparatus. Furthermore, a method is to be created, which largely re-supplied the required heat by a regenerative process to the process, as well as a device that allows such a process management.
  • a device for cracking gases with a supply line for a carbon-containing gas by means of which the gas is fed to a first heat exchanger with a bed of thermal storage mass, a downstream in the flow direction of the gas arranged first combustion chamber, the - a particular controllable and preferably controllable - supply means for another, oxygen-containing gas, by means of which by substoichiometric oxygen supply partial oxidation of the carbonaceous gas takes place, and a downstream in the flow direction of the gas of the first combustion chamber reactor, a bed of a catalytically active material for the catalytic splitting of impurities of the carbon-containing gas dissolved, which is characterized in that in the flow direction of the carbonaceous gas to the reactor below a second combustion chamber with a particular st euerbaren and preferably adjustable feed device for an oxygen-containing gas, by means of which substoichiometric oxygen supply partial oxidation of the catalytically treated carbonaceous gas takes place, and this combustion chamber in the flow direction
  • a combustion chamber is supplied in which the temperature setting by - preferably - permanent, substoichiometric injection of oxygen-containing gases.
  • this combustion chamber is at least before the gas enters the reactor in which a catalytic cracking of impurities located in the gas is provided, at least partial thermal cracking of the tars contained in the gas possible.
  • the thermally treated and partially oxidized gas remaining tars and other impurities are catalytically cleaved by the bed located in the reactor of the catalytically active material.
  • the gas can be supplied to a further combustion chamber, in which the temperature is brought again by sub-stoichiometric oxygen injection in a predetermined range or maintained in this area. From this second combustion chamber, the gas is - at least indirectly - discharged into a second heat exchanger.
  • the reactor preferably offers the possibility of supplying additional substances and in particular catalytically active substances (such as dolomite or nickel-containing substances or materials). Therefore, advantageously, the reactor has a supply device for supplying additional substances.
  • the Applicant reserves the right to claim protection for such a reactorless design.
  • the first bed or the first heat exchanger preferably acts as a heat donor by which the temperature of the gas is increased even before flowing into the first combustion chamber.
  • the second bed or the second heat exchanger preferably serves as a heat acceptor and is heated by the energy contained in the purified (and partially oxidized) gas. By supplying the cold raw gas to the first heat exchanger, this cools continuously, whereas the second heat exchanger is heated continuously by the supply of the hot clean gas. If the bed in the first heat exchanger is cooled below a minimum temperature and / or the bed in the second heat exchanger is heated to such an extent that the gas flowing through is not sufficiently cooled, the flow profile can be reversed by appropriate valve control, at least in the two beds and in the area between them. whereby a regenerative process is provided and thermal energy stored in the second bed is largely re-supplied to the process.
  • the bulk volumes of both beds are preferably designed so that the gas is heated at a heating rate of at least 2000 K / s, preferably 3000 K / s and more preferably greater than 4000 K / s.
  • a heating rate of at least 2000 K / s, preferably 3000 K / s and more preferably greater than 4000 K / s.
  • the device is suitable for carrying out a regenerative cracking process.
  • a flow reversal must take place in certain time steps.
  • This is preferably realized by corresponding valves in the gas lines.
  • the double execution of beds and combustion chambers allows the gas - regardless of the direction of flow - can first pass through a bed and then through a combustion chamber before it enters the reactor.
  • the gas is preheated and brought in the combustion chamber by partial oxidation to the desired temperature and thereby impurities such. Tars already at least partially removed.
  • the gas can also be brought to a desired temperature, again independently of the direction of flow, after leaving the reactor and the endothermic cracking reaction carried out therein in another combustion chamber, again by partial oxidation.
  • the heat energy present in the gas can be used to heat the heat storage medium in the second heat exchanger.
  • the thermal energy for the cracking reactions can be provided by the two combustion chambers and by the heat of reaction released in each case due to the partial oxidation and, on the other hand, the heat losses of the plant can be compensated for.
  • At least one bed, but preferably both beds are at least partially flowed through radially by the gas.
  • the bulk material is preferably surrounded by a cylindrical cold grid and a likewise cylindrical hot grid.
  • conventional bulk material regenerators as known from the prior art, can be used. Such regenerated bulk regenerators are therefore particularly suitable, as they allow high temperature gradients in the bed and thus high heating rates of at least 2000 K / s can be realized.
  • a portion of the dust contained in the gas is retained by the storage mass.
  • appropriate measures must be taken. It is therefore preferred that at least a part of a Storage mass of a bed of at least one heat exchanger for its purification - preferably discontinuously - particularly preferably pneumatically removable from the device and can be returned.
  • the bulk material is preferably withdrawn from the bottom of the bulk material reactor, preferably transported pneumatically upwards and returned to the regenerator after cleaning.
  • the adhering to the bulk dust can be separated, for example by means of a cyclone.
  • the storage mass (after the removal and cleaning described above) in a hot zone of a bed traceable. Since the storage mass is preferably taken from a cool zone of a bed, so a continuous exchange and thus a continuous cleaning of the storage mass is possible.
  • a conveyor for conveying the storage mass is advantageously provided.
  • a delivery opening for carrying out the storage mass is provided from at least one heat exchanger, and preferably also a feed opening in order to supply the storage mass of the device and in particular a heat exchanger and / or the reactor.
  • the bulk material recirculation air, diluted air or other oxygen-containing gases are used as the carrier stream.
  • the oxygen can then react with the optionally adherent coke and / or other dusts or impurities to C0 2 . This ensures that coke residues are burned off during the transport phase.
  • an additional container can be interposed for burning off the bed, in which the bulk material is first collected and in which the burnout preferably takes place discontinuously.
  • the device Since the heat in the presented method or in the corresponding device is regeneratively recovered, it may happen when switching the flow direction that not yet purified gas enters the lines of the already conditioned gas. Therefore, according to a particularly advantageous embodiment, the device has a third bed of thermal storage mass. Through this third heat storage bulk a flushing of the first and second bed is possible. This can be done, for example, by reversing the flow on the line section following the reactor in the flow direction of the gas (the gas thus now flows through this line in the direction of the reactor), the gas after However, the cracking leaves the reactor through the third bed and so no dust or other contaminants from the bed, which was previously used to heat the gas before being fed to the reactor, in the discharge line or product gas line or clean gas line can transport.
  • the storage mass of the third bed is preferably designed so that the pressure drop over this bed is the same size as the pressure drop over the first or second bed. Should the volume of the third bed not be equal to the first and second bed, the pressure loss can be equalized, for example, by adjusting the particle size of the third bed and / or by varying the particle geometry of the third bed.
  • a further preferred embodiment is characterized in that the third bed is constructed axially and that it is connected to the reactor.
  • the reactor and the third bed may in particular be arranged in the same housing. It is preferred that the reactor is arranged with the reaction bed above the third bed. It may be advantageous that between the third bed (the third bed) and the reactor or the reaction bed, a further layer is arranged for isolation. For this purpose, a material with a low thermal conductivity is preferred.
  • this insulation layer can be designed from honeycomb stones.
  • the third bed is so incorporated into a pipe system of the device that they irrespective of the direction of flow of the gas through the first and second bed and / or the first and second heat exchanger only of a purge gas and / or gas from the reactor can be flowed through.
  • the switching between the beds is preferably realized so that the third bed is always acted upon only with hot or cold pure and / or purge gas.
  • this bed the adhesion of dust is avoided and / or the formation of coke suppressed as much as possible.
  • the device and the method can be simplified and operated more cost-effectively, since in this (third) bed means for a circulation promotion (for dust removal) omitted.
  • the beds come as a heat storage honeycomb or pebbles (also called Pebbles) in a fixed bed used.
  • the balls any kind of shapes can be used, such as calipers or Raschig rings.
  • the diameter of the balls is freely selectable, whereby smaller balls increase the specific surface per volume, which has a positive influence on the heat transfer.
  • the pebbles, honeycomb body or similar can be made, for example, from inert alumina (Al 2 0 3 ). It may be advantageous to mix the alumina pebbles with catalytically active substances, such as cobalt, nickel, chromium or their oxides or sulfides.
  • olivine is a suitable storage material, as this has in contrast to dolomite or limestone sufficient mechanical stability and abrasion resistance, so that it can be used for a circulation promotion.
  • Ni catalysts tend to coke heavily at high tar loadings> 2 g / Nm 3 , so that it may be advantageous to switch a layer of dolomite and / or olivine before and after this layer.
  • the device has a purge gas feed line, by means of which at least one bed or a heat exchanger, preferably all beds or heat exchangers, a purge gas can be fed.
  • a purge gas can be fed.
  • cracked gas, cracked gas, inert gas or steam can be used. Cracked gas can be returned to the system via a blower, for example.
  • Particularly preferred is water vapor.
  • the stated object is further achieved by a method for cracking gases, in which a carbon-containing gas is first fed to a first heat exchanger with a bed of thermal storage mass, then fed to a first combustion chamber in which by substoichiometric oxygen supply (which in particular through a controllable and preferentially controllable feeder takes place) of a different oxygen-containing gas, a partial oxidation of the carbon-containing gas is carried out, and subsequently the carbonaceous gas is introduced into a reactor, which preferably has a bed of a catalytically active material for catalytic cracking of carbonaceous gas contaminants, wherein the carbonaceous gas is fed after treatment in the reactor of a second combustion chamber, in which by substoichiometric oxygen supply (which takes place in particular by a controllable and preferably controllable feeder) a partial oxidation of the carbonaceous gas, and coming from this combustion chamber by a second heat exchanger (which preferably has a bed of a thermal storage mass), wherein the flow direction of the carbon
  • a third storage mass is temporarily added, preferably in such a way that the gas flows through the third storage mass.
  • the carbonaceous gas passed through is heated at a rate of at least 2000 K / s, preferably at least 3000 K / s and more preferably at least 4000 K / s is heated.
  • the substantial decoupling of heating zone and reaction zone is particularly advantageous.
  • the catalytically active substances can be accommodated in an amount sufficient to ensure high residence times in a temperature zone in which they are particularly active.
  • the coking rate during heating can be further reduced.
  • the storage mass can be designed specifically for thermal requirements without having to consider reaction kinetic parameters.
  • part of the storage mass is preferably withdrawn discontinuously and cleaned and returned again. More preferably, for the purpose of dust separation, the promotion of the part of the storage mass is pneumatic. Even more preferably, carbon deposits adhering to the bulk material are burned off.
  • the device is also distinguished by the fact that the third storage mass is accommodated in the same vessel in which the reaction bed is accommodated. More preferably, the third storage mass is acted upon only with hot cracked gas and purge gas.
  • gas or water vapor cracked in the apparatus is used as the purge gas.
  • Fig. 2 shows a preferred embodiment of the device with additional third bed and Fig. 3: a particular circuit form of the embodiment shown in Figure 2.
  • FIG. 1 shows a schematic structure of a device for cracking gases. 1 is also a flow chart of the process. Gas is supplied from a main supply line 1 via a valve 3 to the reactor either via the supply line V and via an exhaust line 2 "or after a flow reversal via a supply line 1" discharged via the exhaust pipe 2 '. Via a valve 4 and a main discharge line 2, the purified gas can be supplied to another use (not shown). The position of the valves 3 and 4 is - preferably periodically - changed.
  • the gas to be purified flows through a heat exchanger 5 with a bed in which it is heated at a rate of at least 2000 K / s, into a combustion chamber 6, after which it is fed to a reaction bed 7, in which the tars contained in the gas are reacted , Subsequently, the gas flows through a further combustion chamber 8 and a heat exchanger 9 with a bed of the reactor.
  • the bed 5 serves as a heat donor
  • the bed 9 as a heat acceptor.
  • oxygen-containing gas is injected substoichiometrically via the lines 10 and 1 1.
  • This can be, for example, air or, with particular advantage, pure oxygen.
  • the beds 5 and 9 are preferably flowed through radially by the gas.
  • a portion of a bed can be discontinuously withdrawn, freed from adhering dust and then returned to the bed (not shown).
  • the transport of the bed takes place pneumatically, so that the dust is removed solely by the mechanical movement of the bulk material.
  • adhering coke burned by means of oxygen-containing gases (eg air or diluted air).
  • the return of the discharged part of the bed is preferably realized so that the bulk material is introduced specifically in the hot zone of the bed, as close to the combustion chamber, so that still adhering coke in situ due to the prevailing reaction conditions there Will get removed.
  • FIG. 2 shows a preferred embodiment of the device with additional third bed 12.
  • the one supplied via main supply line 1 flows Gas stream over the bed 5, is thereby heated and thus passes into the combustion chamber 6.
  • the temperature is controlled by the addition of oxygen and / or oxygen-containing gases ..
  • the gas is then passed through a reaction bed 7, at which the tars are catalytically reacted.
  • the gas stream is passed into a combustion chamber 8, in which the temperature is brought to the level in the combustion chamber 6 by adding oxygen again, in particular by covering the heat losses due to the endothermic cracking / reforming reactions is available for further processing steps.
  • a third bed 12 for the purpose of flushing.
  • This can be carried out in a separate vessel, but particularly advantageous is the arrangement of the third bed 12 in the same vessel in which the reaction bed 7 is arranged.
  • the third bed 12 also serves to fix the reaction bed 7.
  • FIG. 3 shows a special circuit form of the embodiment shown in FIG.
  • the bed 5 is acted upon via the purge line 13 with purge gas.
  • valve 14 In order to prevent the bed 12 from heating up in the flushing times and thus reducing the efficiency of the installation, the valve 14 "'is to be opened for a certain period of time for reasons of heat balance, which is always possible if the bed 12 does not contain hot gas is flowed through.
  • the first heat exchanger 5 can be cleaned by opening the valve 14' with purge gas. not shown) of the bed.
  • valve 4 "' can be closed and valve 3' opened, in the opposite direction of flow in the area of the heat exchangers 5, 9, the combustion chambers 6, 8, and the reactor 7 in the flow direction shown in FIG To achieve flow of the gas.
  • insulating layer e.g. honeycombs

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Combustion & Propulsion (AREA)
  • Inorganic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Industrial Gases (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

L'invention concerne un dispositif de craquage de gaz, comprenant une conduite d'alimentation (1) pour un gaz contenant du carbone, au moyen de laquelle le gaz peut être amené à un premier échangeur de chaleur (5, 9) contenant une charge d'une masse d'accumulation thermique; une première chambre de combustion (6, 8) disposée en aval dans le sens d'écoulement du gaz et comportant en particulier un système d'alimentation réglable pour un autre gaz contenant de l'oxygène, au moyen duquel une oxydation partielle du gaz contenant du carbone est effectuée par un apport d'oxygène sous-stœchiométrique; et un réacteur (7), disposé en aval de la première chambre de combustion (6, 8) dans le sens d'écoulement du gaz, qui contient une charge d'un matériau ayant une action catalytique afin de dissocier catalytiquement les impuretés du gaz contenant du carbone. Selon l'invention, une seconde chambre de combustion (6, 8) est disposée en aval du réacteur (7) dans le sens d'écoulement du gaz contenant du carbone. Cette chambre de combustion comporte un système d'alimentation, en particulier réglable, pour un gaz contenant de l'oxygène, au moyen duquel une oxydation partielle du gaz contenant du carbone traité catalytiquement est effectuée par un apport d'oxygène sous-stœchiométrique, et un second échangeur de chaleur (5, 9) contenant une charge d'une masse d'accumulation thermique est disposé en aval de ladite seconde chambre de combustion dans le sens d'écoulement du gaz. Le sens d'écoulement du gaz contenant du carbone peut être inversé au moins dans une zone englobant les premier et second échangeurs de chaleur (5, 9), les première et seconde chambres de combustion (6, 8) et le réacteur (7).
EP13805823.5A 2012-12-06 2013-12-06 Dispositif et procédé de craquage de gaz Withdrawn EP2928991A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102012111900.7A DE102012111900A1 (de) 2012-12-06 2012-12-06 Vorrichtung und Verfahren zum Cracken von Gasen
PCT/EP2013/075858 WO2014087000A1 (fr) 2012-12-06 2013-12-06 Dispositif et procédé de craquage de gaz

Publications (1)

Publication Number Publication Date
EP2928991A1 true EP2928991A1 (fr) 2015-10-14

Family

ID=49766056

Family Applications (1)

Application Number Title Priority Date Filing Date
EP13805823.5A Withdrawn EP2928991A1 (fr) 2012-12-06 2013-12-06 Dispositif et procédé de craquage de gaz

Country Status (5)

Country Link
US (1) US9533274B2 (fr)
EP (1) EP2928991A1 (fr)
CN (1) CN104955924A (fr)
DE (1) DE102012111900A1 (fr)
WO (1) WO2014087000A1 (fr)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102021129812A1 (de) 2021-11-16 2023-05-17 HiTES Holding GmbH Verfahren und Vorrichtung zum Erzeugen von Wasserstoff
DE102021129804A1 (de) 2021-11-16 2023-05-17 HiTES Holding GmbH Verfahren und Vorrichtung zum Erzeugen von Wasserstoff
DE102021129810A1 (de) 2021-11-16 2023-05-17 HiTES Holding GmbH Verfahren und Vorrichtung zum Erzeugen von Wasserstoff

Families Citing this family (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110072607A (zh) 2016-10-06 2019-07-30 利腾股份有限公司 具有气固分离的微波反应器系统
US9812295B1 (en) 2016-11-15 2017-11-07 Lyten, Inc. Microwave chemical processing
US9767992B1 (en) 2017-02-09 2017-09-19 Lyten, Inc. Microwave chemical processing reactor
US9997334B1 (en) 2017-02-09 2018-06-12 Lyten, Inc. Seedless particles with carbon allotropes
WO2018169889A1 (fr) 2017-03-16 2018-09-20 Lyten, Inc. Intégration de carbone et d'élastomère
US10920035B2 (en) 2017-03-16 2021-02-16 Lyten, Inc. Tuning deformation hysteresis in tires using graphene
US9862606B1 (en) 2017-03-27 2018-01-09 Lyten, Inc. Carbon allotropes
US9862602B1 (en) * 2017-03-27 2018-01-09 Lyten, Inc. Cracking of a process gas
US10465128B2 (en) 2017-09-20 2019-11-05 Lyten, Inc. Cracking of a process gas
US10756334B2 (en) 2017-12-22 2020-08-25 Lyten, Inc. Structured composite materials
US10644368B2 (en) 2018-01-16 2020-05-05 Lyten, Inc. Pressure barrier comprising a transparent microwave window providing a pressure difference on opposite sides of the window
WO2024150163A1 (fr) * 2023-01-12 2024-07-18 Tenova S.P.A. Installation et procédé de production à haut rendement d'hydrogène par pyrolyse

Family Cites Families (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2885455A (en) * 1956-12-19 1959-05-05 Pure Oil Co Process for chemical pyrolysis
DE19521673C2 (de) 1995-06-14 1998-07-02 Atz Evus Applikations & Tech Verfahren zur regenerativen Abluftreinigung
US6299994B1 (en) * 1999-06-18 2001-10-09 Uop Llc Process for providing a pure hydrogen stream for use with fuel cells
NL1016019C2 (nl) 2000-08-25 2002-02-26 B T G B V Werkwijze en inrichting voor het verwerken van dierlijke mest.
NL1016975C2 (nl) 2000-12-22 2002-06-25 Biomass Technology Group B V Werkwijze voor het uitvoeren van een kraakreactie in een omkeerstroomreactor.
DE102004026646B4 (de) 2004-06-01 2007-12-13 Applikations- Und Technikzentrum Für Energieverfahrens-, Umwelt- Und Strömungstechnik (Atz-Evus) Verfahren zur thermischen Entsorgung schadstoffhaltiger Substanzen
US7846401B2 (en) * 2005-12-23 2010-12-07 Exxonmobil Research And Engineering Company Controlled combustion for regenerative reactors
CN101346176B (zh) 2005-12-23 2012-07-18 埃克森美孚化学专利公司 甲烷转化为更高级烃
CN101462694B (zh) 2007-12-19 2011-04-20 中国科学院大连化学物理研究所 一种微型化的甲醇自热重整制氢集成装置和制氢方法
DE102008021084A1 (de) 2008-04-28 2009-10-29 Süd-Chemie AG Verwendung eines Katalysators auf Edelmetallbasis zur Verringerung des Teergehalts in Gasen aus Vergasungsprozessen
CN101955804A (zh) 2010-09-16 2011-01-26 合肥天焱绿色能源开发有限公司 固体生物质气化系统及其工艺
US8703064B2 (en) * 2011-04-08 2014-04-22 Wpt Llc Hydrocabon cracking furnace with steam addition to lower mono-nitrogen oxide emissions

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102021129812A1 (de) 2021-11-16 2023-05-17 HiTES Holding GmbH Verfahren und Vorrichtung zum Erzeugen von Wasserstoff
DE102021129804A1 (de) 2021-11-16 2023-05-17 HiTES Holding GmbH Verfahren und Vorrichtung zum Erzeugen von Wasserstoff
DE102021129810A1 (de) 2021-11-16 2023-05-17 HiTES Holding GmbH Verfahren und Vorrichtung zum Erzeugen von Wasserstoff
WO2023088873A1 (fr) 2021-11-16 2023-05-25 HiTES Holding GmbH Procédé et dispositif de production d'hydrogène
WO2023088871A1 (fr) 2021-11-16 2023-05-25 HiTES Holding GmbH Procédé et dispositif de production d'hydrogène
WO2023088878A1 (fr) 2021-11-16 2023-05-25 HiTES Holding GmbH Procédé et dispositif de production d'hydrogène

Also Published As

Publication number Publication date
US9533274B2 (en) 2017-01-03
WO2014087000A1 (fr) 2014-06-12
CN104955924A (zh) 2015-09-30
DE102012111900A1 (de) 2014-06-26
US20160059197A1 (en) 2016-03-03

Similar Documents

Publication Publication Date Title
EP2928991A1 (fr) Dispositif et procédé de craquage de gaz
EP2780105B1 (fr) Réacteur à tubes et calandre pour la mise en oeuvre de réactions catalytiques en phase gazeuse
DE69519465T2 (de) Tranportteiloxidationsmethode
DE102013018074B3 (de) Hochofen und verfahren zum betrieb eines hochofens
WO2010003968A2 (fr) Procédé et dispositif pour produire du gaz de synthèse à faible teneur en goudrons à partir de biomasse
DE102007062414A1 (de) Autothermes Verfahren zur kontinuierlichen Vergasung von kohlenstoffreichen Substanzen
EP1637574A1 (fr) Procédé et appareillage pour la gazéification thermique de composés contenant des hydrocarbures
WO2007118736A1 (fr) Procédé et dispositif d'épuration intégrée des gaz chauffés des constituants gazeux et pulvérulents de gaz de synthèse
WO2011110138A1 (fr) Procédé et dispositif pour produire du gaz de synthèse et pour faire fonctionner un moteur à combustion interne au moyen de ce gaz
EP1950272A1 (fr) Procédé et dispositif destinés à la transformation thermique de pellets ou de copeaux de bois
EP1337607B1 (fr) Procede de gazeification de substances organiques en un etat liquide a pateux, et de melanges de telles substances
DE102009047445A1 (de) Anlage zum Erzeugen eines Produktgases aus organischen Einsatzstoffen
DE202014005809U1 (de) Vorrichtung zur Reinigung und Gewinnung von energiehaltigen Gasen
EP3580312B1 (fr) Preparation de syntheseges a partir de substances carbones au moyen d'une procedure combiné co-courant et contre-courant
WO2011015339A1 (fr) Procédé et dispositif de refroidissement d'une matière solide en vrac à grain fin avec échange simultané du gaz d'espace vide contenu dans celle-ci
WO2014087001A1 (fr) Procédé et dispositif de craquage de gaz
EP3792216B1 (fr) Intégration thermique lors de la génération des gaz de synthèse par oxydation partielle
EP3214155B1 (fr) Procédé pour la production de gaz de synthèse pour la combustion dans un moteur à combustion interne.
EP1399527B1 (fr) Procede et dispositif pour pyrolyser et gazeifier des melanges de matieres a composants organiques
DE102017210044A1 (de) Nachbehandlungsanordnung und Verfahren zum Nachbehandeln von zumindest Gasen stromab einer Wirbelschichtvergasung sowie Logikeinheit und Verwendung
DE102009057109A1 (de) Simultane Herstellung von teerfreiem Synthesegas und Kohlenstoff aus Biomasse
DE10228100B4 (de) Verfahren und Vorrichtung zur Pyrolyse und Vergasung von Stoffgemischen, die organische Bestandteile enthalten
DE102021134442B4 (de) Anlage zur Erzeugung eines Synthesegases und Verfahren zum Betreiben derselben
WO2014012651A1 (fr) Gazéification à contre-courant/co-courant de substances riches en carbone
DE102013020889A1 (de) Verfahren und Anlage zur zumindest teilweisen Vergasung von festem, organischem Einsatzmaterial

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

17P Request for examination filed

Effective date: 20150617

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR

AX Request for extension of the european patent

Extension state: BA ME

DAX Request for extension of the european patent (deleted)
STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE APPLICATION IS DEEMED TO BE WITHDRAWN

18D Application deemed to be withdrawn

Effective date: 20170701