EP2480632A2 - Réacteur de gaz de synthèse à nuage de coke chauffé - Google Patents

Réacteur de gaz de synthèse à nuage de coke chauffé

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Publication number
EP2480632A2
EP2480632A2 EP10757153A EP10757153A EP2480632A2 EP 2480632 A2 EP2480632 A2 EP 2480632A2 EP 10757153 A EP10757153 A EP 10757153A EP 10757153 A EP10757153 A EP 10757153A EP 2480632 A2 EP2480632 A2 EP 2480632A2
Authority
EP
European Patent Office
Prior art keywords
reactor
coke
gas
pyrolysis
cloud
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Withdrawn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
EP10757153A
Other languages
German (de)
English (en)
Inventor
Karl-Heinz Tetzlaff
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.)
Individual
Original Assignee
Individual
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 Individual filed Critical Individual
Publication of EP2480632A2 publication Critical patent/EP2480632A2/fr
Withdrawn legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
    • C10J3/60—Processes
    • C10J3/64—Processes with decomposition of the distillation products
    • C10J3/66—Processes with decomposition of the distillation products by introducing them into the gasification zone
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B19/00—Heating of coke ovens by electrical means
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
    • C10B47/18—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with moving charge
    • C10B47/22—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with moving charge in dispersed form
    • C10B47/24—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with moving charge in dispersed form according to the "fluidised bed" technique
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
    • C10B53/02—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of cellulose-containing material
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/482—Gasifiers with stationary fluidised bed
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/82—Gas withdrawal means
    • C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
    • C10K3/001—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by thermal treatment
    • C10K3/003—Reducing the tar content
    • C10K3/006—Reducing the tar content by steam reforming
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/0916—Biomass
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0956—Air or oxygen enriched air
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0959—Oxygen
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0973—Water
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/12—Heating the gasifier
    • C10J2300/1269—Heating the gasifier by radiating device, e.g. radiant tubes
    • C10J2300/1276—Heating the gasifier by radiating device, e.g. radiant tubes by electricity, e.g. resistor heating
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1684—Integration of gasification processes with another plant or parts within the plant with electrolysis of water
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1846—Partial oxidation, i.e. injection of air or oxygen only
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/10—Biofuels, e.g. bio-diesel
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/141—Feedstock
    • Y02P20/145—Feedstock the feedstock being materials of biological origin

Definitions

  • the invention relates to a device for the production of synthesis gas from essentially solid fuels.
  • the invention relates to a process for the production of synthesis gas from im
  • Substantially solid fuels preferably biomass, by steam reforming.
  • the synthesis gas can be produced in a two-stage process.
  • Coke particles contained ashes can melt due to the resulting high temperatures. This restricts the gasifiable biomasses to woody biomasses because their ashes have a higher melting point.
  • Fluidized beds can be reduced. These fluidized beds are operated with inert bed material. The expenditure on equipment is very high.
  • the invention is therefore based on the object, a
  • At least one coke cloud reactor is provided, wherein the coke cloud reactor has at least one heating device for the catalytic cracking of the tars of the pyrolysis gas.
  • a substantially solid fuel is decomposed in at least one pyrolysis reactor into pyrolysis gas and coke, the coke
  • the coke particles thus obtained are carried by the pyrolysis gas in at least one coke cloud reactor, which is heated by at least one heating device, so that the tar contained in the pyrolysis gas is catalytically reacted to the coke particles. It comes to a
  • Pyrolysis gas can also be a thermal cleavage of the tars.
  • the thermal cracking of the tars takes place only at temperatures of for example 1300 ° C to 1600 ° C.
  • the catalytic conversion of coke particles can already at temperatures of about 700 ° C to 1000 ° C,
  • Synthesis gas can be obtained.
  • Kokswolke a very good heat and mass transfer is achieved, which can be used by means of the heater and the catalytic effect of the coke particles, in a simple manner a substantially
  • the cleavage of the tars can also be carried out a thermal cleavage of tars. Since the temperature required for a thermal conversion of the tars may be above the ash melting point, in procedural terms at least one appreciable part,
  • the majority of the tars are catalytically reacted. It is preferred if the tars, im
  • substantially solid fuels are understood to mean fuels which are at
  • biomass is used as fuel.
  • steam reforming may also be carried out at least partially, in particular if the at least one pyrolysis reactor
  • Water preferably in the form of water vapor, is supplied and / or the biomass has a corresponding moisture.
  • coconut cloud stands for an accumulation of
  • Coke particles entrained or at least suspended in a pyrolysis gas stream Coke particles entrained or at least suspended in a pyrolysis gas stream.
  • Coke particles are produced by pyrolysis of a solid fuel, in particular of biomass, in at least one
  • Pyrolysis reactor formed. If necessary, a comminution of the coke particles can take place in parallel or subsequently. In the at least one pyrolysis reactor and the pyrolysis gas is generated which keeps the coke particles in suspension or transported further in the flow direction of the pyrolysis gas.
  • the pyrolysis gas is usually tarry.
  • Tars are high molecular weight compounds with a correspondingly high boiling point. Although many of these compounds have boiling points below 250 ° C, they can cause problems. So-called primary tars are made by exceeding the boiling point of the biomass
  • secondary tars such as alkylated mono- and
  • Diaromatics including the heteroaromatic consist At high temperatures are increasingly also as
  • Höchtemperatur- or Rekombinationsteere designated tertiary tars such as benzene, naphthalene, phenanthrene, pyrene, benzopyrene in the pyrolysis gas, which are mainly formed by recombination of secondary tars.
  • a coke cloud reactor is understood to mean one which has a reaction space into which the coke cloud can penetrate and in which the coke particles of the
  • Gas flow are kept at least in the balance.
  • a bed material made of inert bedding is in the
  • coconut cloud reactor dispensed.
  • coke and any reaction products are in the form of solids
  • Kokswolkenreaktor can therefore be regarded as a synthesis gas reactor. Furthermore, a catalytic reaction of the tars contained in the gas stream takes place on the hot coke particles of the coke cloud. This reaction requires heat, for which purpose at least one heating device is provided in the coke cloud reactor.
  • pyrolysis gas leaving gas referred to as pyrolysis gas.
  • the gas in the coke cloud reactor is also called pyrolysis gas.
  • composition of the pyrolysis gas differs depending on where the pyrolysis gas is in the apparatus. However, for ease of understanding, the number of terms used should be kept low.
  • Kokswolkenreaktor arranged above the pyrolysis reactor such that the coke particles carried by the pyrolysis gas in the vertical direction of the pyrolysis reactor in the
  • Get coconut cloud reactor A purely vertical direction is preferred. However, an oblique, upward-pointing direction can still be included. The more vertical the direction the easier the device can be constructed and the lower the risk of deposits of
  • Coke particles in the device are Coke particles in the device.
  • the pyrolysis reactor and the coke cloud reactor need not be stacked. Both reactors can in principle also be arranged next to one another.
  • the pyrolysis gas carrying the coke particles can also be led to the side and fed to the lower part of the coke cloud reactor.
  • the flow rate of the pyrolysis gas should be large enough to segregation and / or
  • the pyrolysis reactor is a fluidized bed reactor with an inert bed material. Then the
  • the pyrolysis reactor has a stationary fluidized bed, this is favorable for the comminution of the coke.
  • the resulting small coke particles are sufficiently heated up to the core thereof, so that the primary tars emerge in the pyrolysis reactor and not in the coke cloud reactor.
  • most of the tars in the stationary fluidized bed are expelled from the coke.
  • an axial arrangement can also be understood to mean one in which the centers of the reactors are arranged approximately in alignment with one another.
  • At least one constriction of the free flow cross-section may locally be deliberately provided locally in the coke cloud reactor in order to subdivide the reaction space into corresponding sections and thus prevent backmixing as well as a short-circuit flow.
  • the at least one taper of the free flow cross section can be created for simplicity by at least one perforated plate and / or a nozzle bottom.
  • this may have a gas-permeable, porous region.
  • the heater may have a plurality of provided within the Kokswolkenreaktors tubes.
  • the heater may have a plurality of provided within the Kokswolkenreaktors tubes.
  • the heater may, if necessary, have a superficial tarerspaltering catalyst.
  • the catalytic conversion of the tars to the coke particles can still be supported.
  • the catalytic material can be provided on the gas-permeable, porous region, in particular on its pore system.
  • Kokswolkenreaktors then the synthesis gas is withdrawn. If the fluidizing gas has sufficient moisture for steam reforming, no further gas supply is required.
  • the coke cloud reactor When the coke cloud reactor is divided into various sections, it is preferable that the coke particles successively pass through the plurality of coke clouds formed in the serially arranged sections.
  • the coke cloud reactor can thus be regarded as a stirred tank cascade.
  • the heating of the coke cloud reactor is preferably carried out by a heating device arranged in the cross section of the coke cloud reactor, whereby a good heat transfer is achieved.
  • a cavity of the heater In order to increase the heat input into the Kokswolkenreaktor, a cavity of the heater a
  • oxygen-containing gas which oxidizes pyrolysis gas in a porous section of the heater.
  • Pyrolysis gas are sucked into the porous section, without this part of the pyrolysis gas would have to be deducted.
  • the tar contained in the pyrolysis gas in the porous portion of the heating device i. be implemented in its pore system, there provided on catalytic material. This is especially true if the mere increase in temperature for a corresponding implementation of the tars alone is insufficient.
  • the heating device can be arranged at least partially in the cross section of the coke cloud reactor. The heater then reduces the free flow cross-section for the cocaine cloud and can simultaneously a large
  • the coke cloud preferably flows similar to one
  • Kokswolkenreaktor can be considered reaction technology approximately as a tubular reactor.
  • the biomass is used in one embodiment in the
  • Kokswolkenreaktor is therefore preferably above the
  • Pyrolysis reactor arranged so that the pyrolysis gas with the Coking only has to flow upwards. Settling of coke particles in plant parts between the pyrolysis reactor and the synthesis gas reactor can thus be avoided.
  • the pyrolysis gas is reacted by means of a heater to at least largely tar-free synthesis gas.
  • the tars contained in the pyrolysis gas are catalytically destroyed on the hot coke particles, without the ash of the coke particles is melted.
  • the fluidizing gas is preferably that through the
  • Fluidized bed of flowing gas or gas mixture for swirling the bed material Under the actual synthesis gas, the product gas is understood, preferably a
  • the solid fuel or biomass are first pyrolyzed, ie decomposed into pyrolysis gas and coke.
  • the coke can then be crushed. This can be done for example by a method and an apparatus according to DE 198 07 988 AI. However, it is simpler, the pyrolysis in a, preferably stationary, fluidized bed with inert
  • Bed material perform.
  • the pyrolysis and the comminution of the coke are carried out simultaneously and in one apparatus or, if required, in a reactor, the comminution of the coke essentially taking place by abrasion with the inert bed material of the pyrolysis reactor.
  • the bed material is especially sand in question.
  • the advantage a stationary fluidized bed is also that the device according to the invention can be integrated into this apparatus.
  • Conditionally suitable for the pyrolysis is a
  • Fluidized bed reactor with circulating fluidized bed Depending on the mode of operation, coarser coke particles which are less suitable for the process according to the invention are then produced.
  • the temperature of the pyrolysis i. the temperature in the
  • Pyrolysis reactor may be between 400 ° C and 1000 ° C, preferably between 600 ° C to 850 ° C.
  • the temperature is preferably so high that both a pyrolysis and a steam reforming takes place in the pyrolysis reactor.
  • Reaction conditions are always to be selected in a manner known per se so that coke is still available for the coke cloud reactor.
  • the pyrolysis gas is introduced together with the coke particles in the heatable coke cloud reactor.
  • the coke particles should preferably be so fine that they are from the
  • the coke particles can be carried gas flow.
  • the coke particles can be carried gas flow.
  • the particles should preferably not be greater than 3 mm, because with larger particles, a high gas velocity must be selected to the coke particles from the
  • Transport pyrolysis reactor in the coconut cloud reactor has the consequence that the residence time in the coke cloud reactor is greatly reduced.
  • the particle size should be less than 1 mm.
  • the coke cloud reactor can be arranged above the pyrolysis reactor.
  • the reaction zone of the coke cloud reactor can begin directly above the pyrolysis reactor.
  • the coke particles can namely discharged from the pyrolysis gas against gravity from the pyrolysis reactor and the
  • Kokswolkenreaktor be supplied.
  • the coke particles ideally flow past the heater of the coke cloud reactor as a plug flow and are on their way to the
  • Preferred is a substantially vertical
  • the flow direction can basically also be slightly oblique. However, horizontal or even pointing in the direction of gravity flow directions are
  • the heating device can have a multiplicity of heating tubes oriented parallel to one another, which form narrow free flow cross sections between each other, as a result of which backmixing (turbulence) is largely avoided. Because of high coke loading of the pyrolysis gas
  • Kokswolkenreaktor be divided by cross-sectional constrictions in several sections. This can be done for example by perforated plates, in which the flow velocity in the holes is so high that no gas can flow back.
  • the Kokswolkenreaktor can then reaction technology as so-called Rhakkesselkaskade, ie series connection of several ideal stirred tank, are considered.
  • Rhakkesselkaskade ie series connection of several ideal stirred tank
  • Coking particles are split catalytically.
  • Heating device to be coated with a catalyst Parts of the heating device coming into contact with the pyrolysis gas can also be made of a catalyst. It is particularly advantageous if the heating device has porous tubes and / or is designed as an electric heater.
  • Nickel can be used as the catalytically active material.
  • Catalysts may be, for example, group VIII nickel-based catalysts
  • Periodic system which also destroy ammonia at the same time.
  • the doping of nickel-based catalysts with MgO, Zr0 2 and / or Zr0 2 -Al 2 0 3 may be advantageous.
  • the mass transfer can be improved by using pulsating pressure changes to the inner cavity of the tubes when using porous tubes.
  • the tubes may preferably be subjected to pressure changes of a frequency of 0.1 to 10,000 heart, preferably 5 to 500 Hz. Because of the absence of an inert bed material, such as sand (Si0 2 ), with potassium and phosphorus contained in the biomass, despite the heating of the coke cloud reactor no
  • Low-melting eutectics can be formed, otherwise problematic biomass can be used with high potassium and / or phosphorus content, whose ashes at
  • Coke particles are preferably predominantly or more preferably substantially by heat radiation. Due to the endothermic reaction in the implementation of
  • the Heater then has at least one porous section in which a portion of the pyrolysis gas is oxidized and heats the heater.
  • Heating device can be connected for example via perforated plates to the power supply, wherein the perforated plates simultaneously divide the reaction space of the coke cloud reactor into individual reaction zones.
  • Heating device is then or by similar measures partially adjustable.
  • the use of electrical energy is preferred because in the future electrical energy is not more valuable than thermal energy.
  • the method according to the invention makes it possible, with little expenditure on equipment, to largely remove tar by means of primary measures.
  • the ash is not melted and can therefore be used as a mineral fertilizer.
  • the heater preferably consists of a plurality of heaters. Heaters may be in the form of plates, tubes and / or rods.
  • Fig. 1 is a Kokswolkenreaktor, which together with a
  • Reactor device is integrated, and
  • Fig. 2 is a heating orcardi the heater of FIG. 1 in a sectional view.
  • Fig. 1 shows a reactor device 1, with a housing 5, in which a Kokswolkenreaktor 11 are included together with a pyrolysis reactor 16.
  • the pyrolysis reactor 16 is formed as a stationary fluidized bed reactor with a fluidized bed 6 of an inert bed material, the upper end of which is marked 8.
  • the nozzle bottom 7 forms the lower end of the fluidized bed 6, in which a designed as an electric heater heater 12 is provided.
  • stationary fluidized bed is heated by the heater 12 to a temperature of about 400 ° C to 1000 ° C, preferably from about 600 ° C to 850 ° C.
  • the pyrolysis of the biomass 2 introduced into the pyrolysis reactor 16 takes place.
  • the fluidized bed 6 is a fluidizing gas 3 supplied, which is the necessary amount
  • the pyrolysis gas i. the gas formed in the pyrolysis reactor 16 together with the in
  • Pyrolysis reactor 16 formed coke particles in the first portion 10 a of the coke cloud reactor 11, which with a
  • Heating device 18 is equipped and is arranged directly above the stationary fluidized bed 6 of the pyrolysis 16. In the illustrated and so far preferred
  • Kokswolkenreaktor 11 provided in a substantially tubular reactor housing one above the other.
  • the maximum size of the coke particles can be determined by selecting the conditions such as grain size, reactor size, throughput, pressure and / or
  • the heating device 18 has a plurality of heating tubes 13.
  • the heating tubes 13 form narrow channels as free
  • Kokswolkenreaktor 11 additionally perforated plates 9a-9c arranged, which divide the Kokswolkenreaktor 11 in the sections 10a to lOd. It could instead of perforated plates 9a- 9c too
  • Nozzle bottoms can be provided.
  • Kokswolkenreaktor 11 could be discharged and so passes as an impurity in the synthesis gas 4 as a product gas.
  • the energy for the heater 18 may come from any source. Shown is an electric heater with vertically arranged tubes 13. To adjust the heating power to the reaction progress, is a separately controllable heating in the individual sections 10b-10d of
  • the steam reforming therefore does not have to be operated so far that the solid fuel, for example in the form of biomass 2, is completely converted to synthesis gas 4 and ash. This may be preferred, but it may be for
  • a heating device 18 comprising porous tubes 13 can be used. These tubes 13 are provided with a pipe connection 17 and have at the end
  • Coconut cloud reactor 11 contained gases. It is also possible to provide the pipes with a pipe connection at each end and to pass the oxygen through.
  • the pyrolysis gas flows into the tubes 13 and meets the oxygen 15.
  • the pyrolysis gas reacts already in the pores with oxygen and heats the tube 13.
  • the oxidized gases can then over the second port can be removed for further use. In this case, so no combustion products get into the
  • Kokswolkenreaktor 11 In this method, however, adherent filter layers can form on the tubes 13. Therefore, these should be replaced from time to time with a pressure change. This method is therefore particularly suitable for the pyrolysis reactor 16, because the tubes 13 are then already scratched free by the bed material in the form of sand.
  • the coke cloud reactor 11 may choose the pressure of the oxygen 15 in the porous tubes 13 to be greater than in the coke cloud reactor 11. Then, the oxygen 15 passes through the pore system of the heater 18 in the Coconut cloud reactor 11 a. This leads to a partial oxidation of the pyrolysis gas and a corresponding

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Materials Engineering (AREA)
  • Thermal Sciences (AREA)
  • Physics & Mathematics (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Dispersion Chemistry (AREA)
  • Industrial Gases (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Hydrogen, Water And Hydrids (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

L'invention concerne un dispositif (1) pour produire un gaz de synthèse (4) à partir de combustibles sensiblement solides, de préférence à partir de biomasse (2), par reformage à la vapeur, comprenant au moins un réacteur de pyrolyse (16) pour former un gaz de pyrolyse contenant des particules de goudron et des particules de coke. Afin de produire un gaz de synthèse qui est sensiblement exempt de goudron de manière simple et peu onéreuse, le dispositif est équipé d'au moins un réacteur à nuage de coke (11), lequel comprend au moins un dispositif de chauffage (18) pour le craquage catalytique du goudron dans les gaz de pyrolyse.
EP10757153A 2009-09-03 2010-09-03 Réacteur de gaz de synthèse à nuage de coke chauffé Withdrawn EP2480632A2 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102009039836A DE102009039836A1 (de) 2009-09-03 2009-09-03 Synthesegasreaktor mit beheizter Kokswolke
PCT/EP2010/005409 WO2011026631A2 (fr) 2009-09-03 2010-09-03 Réacteur de gaz de synthèse à nuage de coke chauffé

Publications (1)

Publication Number Publication Date
EP2480632A2 true EP2480632A2 (fr) 2012-08-01

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EP (1) EP2480632A2 (fr)
DE (1) DE102009039836A1 (fr)
TW (1) TWI522453B (fr)
WO (1) WO2011026631A2 (fr)

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CN112126450B (zh) * 2020-09-29 2021-05-04 华中科技大学 基于波谱分裂的聚光热解催化重整系统及方法
GB202106334D0 (en) * 2021-05-04 2021-06-16 Ucl Business Ltd Thermochemical reactor and process
CN113587107A (zh) * 2021-08-09 2021-11-02 泰安圣智环境技术有限公司 一种生活垃圾热解系统和热解方法

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Publication number Priority date Publication date Assignee Title
DE3635215A1 (de) * 1986-10-16 1988-04-28 Bergwerksverband Gmbh Verfahren zur allothermen kohlevergasung und wirbelbett-gasgenerator zur durchfuehrung des verfahrens
DE19807988B4 (de) 1998-02-26 2007-11-08 Wolf, Bodo, Dr.-Ing. Verfahren zur Abtrennung von flüchtigen Bestandteilen aus festen Brennstoffen
CA2349608A1 (fr) * 1998-11-05 2000-05-18 Ebara Corporation Systeme de production d'energie par gazeification d'un materiau combustible
DE19948332B4 (de) * 1999-10-07 2005-09-22 Steer, Thomas, Dr.-Ing. Verfahren und Vorrichtung zum Gewinnen heizwertreicher Brennstoffe
DE10033453B4 (de) * 2000-07-10 2006-11-02 Herhof Verwaltungsgesellschaft Mbh Verfahren und Vorrichtung zur Verwertung von Stoffen und Stoffgemischen, die organische Bestandteile enthalten
JP3973840B2 (ja) * 2001-01-18 2007-09-12 独立行政法人科学技術振興機構 固形燃料ガス化装置
DE10222604A1 (de) * 2001-07-20 2003-02-06 Bu Bioenergie & Umwelttechnik Vorrichtung und ein Verfahren zur Erzeugung von Gas
EP2017003A1 (fr) * 2007-07-20 2009-01-21 Pall Corporation Élément catalytique
DE102008014799A1 (de) 2008-03-18 2009-09-24 Karl-Heinz Tetzlaff Verfahren und Vorrichtung zur Herstellung von Synthesegas aus Biomasse
DE102008032166A1 (de) 2008-07-08 2010-01-14 Karl-Heinz Tetzlaff Verfahren und Vorrichtung zur Herstellung von teerfreiem Synthesgas aus Biomasse

Non-Patent Citations (2)

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None *
See also references of WO2011026631A2 *

Also Published As

Publication number Publication date
TWI522453B (zh) 2016-02-21
WO2011026631A3 (fr) 2012-06-28
DE102009039836A1 (de) 2011-03-10
WO2011026631A2 (fr) 2011-03-10
TW201113359A (en) 2011-04-16

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