EP2771437A1 - Procédé de fonctionnement d'un réacteur à gazéification - Google Patents

Procédé de fonctionnement d'un réacteur à gazéification

Info

Publication number
EP2771437A1
EP2771437A1 EP12783523.9A EP12783523A EP2771437A1 EP 2771437 A1 EP2771437 A1 EP 2771437A1 EP 12783523 A EP12783523 A EP 12783523A EP 2771437 A1 EP2771437 A1 EP 2771437A1
Authority
EP
European Patent Office
Prior art keywords
gasification
reaction chamber
reactor
controlled
fuel
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Withdrawn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
EP12783523.9A
Other languages
German (de)
English (en)
Inventor
Martin ZUCKERMAIER
Thomas Tschaftary
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.)
LIGENTO GREEN POWER GMBH
Original Assignee
Ligento Green Power GmbH
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 Ligento Green Power GmbH filed Critical Ligento Green Power GmbH
Publication of EP2771437A1 publication Critical patent/EP2771437A1/fr
Withdrawn legal-status Critical Current

Links

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
    • C10J3/72—Other features
    • C10J3/723—Controlling or regulating the gasification process
    • 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
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/20—Apparatus; Plants
    • C10J3/22—Arrangements or dispositions of valves or flues
    • C10J3/24—Arrangements or dispositions of valves or flues to permit flow of gases or vapours other than upwardly through the fuel bed
    • C10J3/26—Arrangements or dispositions of valves or flues to permit flow of gases or vapours other than upwardly through the fuel bed downwardly
    • 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
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/20—Apparatus; Plants
    • C10J3/34—Grates; Mechanical ash-removing devices
    • C10J3/36—Fixed grates
    • 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
    • C10J3/78—High-pressure apparatus
    • 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
    • C10J2300/093—Coal
    • 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
    • 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
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/16—Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]
    • Y02E20/18—Integrated gasification combined cycle [IGCC], e.g. combined with carbon capture and storage [CCS]

Definitions

  • the invention relates to a method for operating a gasification reactor (1) with a reaction chamber (4) for the autothermal and / or allothermal gasification of carbonaceous fuel to useful gases, wherein composition (28), amount (20), pressure (22), speed, Temperature (26) and / or specific outlet pulse of a control inputs (10) of the reaction chamber (4) added gasification variable based on a number of in the reaction chamber (4) determined control variables (30, 32, 34, 36, 38, 40) to be controlled.
  • Such a method is known, for example, from DE 10 2004 020 919 A1.
  • a reactor is generally understood to mean a part of a plant in which chemical reactions of one or more starting materials to one or more products are carried out. Therefore, in this invention, under a gasification reactor, a container is understood to be a part of an installation in which carbonaceous fuel material is converted into useful gases, ie gasified.
  • a useful gas is understood as meaning a substance or a substance mixture which is suitable both itself as fuel for internal combustion engines and also as raw material for further chemical production processes.
  • a carbonaceous fuel material is understood to mean such a material whose carbon contained in the form of an exothermic reaction oxidizes to carbon dioxide (CO 2 ) in air, that is to say it can be burned.
  • the carbonaceous fuel includes in particular
  • biomass in particular biomass, fossil fuels and synthetic organic substances, especially according to carbon-containing plastics.
  • biomass is generally understood to mean any carbonaceous substance which is derived directly or indirectly from physiological processes of living organisms, in particular from plant photosynthesis, is not deprived of the natural carbon cycle and can also be exothermally converted to CO2 by organisms.
  • biomass are fermentation residues, wood, leaves, hay, straw, paper, cardboard, compost, faeces and sewage sludge.
  • fossil fuels are understood to mean those forms of biomass which are located in a geological depression and are thus removed from the natural carbon cycle.
  • fossil fuels are asphalt, tar, bitumen, peat, lignite, hard coal and graphite.
  • a carbonaceous fuel material may also be understood to mean a mixture of different carbonaceous fuel materials, for example biomass, synthetic-organic materials and especially plastics.
  • Another example of a carbonaceous fuel is therefore household waste as a mixture of such fuels.
  • the shape of the carbonaceous fuel is independent of its shape, another example is wood in the form of logs, wood chips of varying size, sawdust or in the form of pellets.
  • the pyrolysis as a purely thermal decomposition of biomass, hard coal and lignite runs predominantly endothermic depending on the oxygen content and the binding of the oxygen. Within the fuel, the pyrolysis may also be exothermic.
  • the pyrolysis of hard coal or brown coal arise in addition to carbon monoxide (CO), hydrogen (H 2 ) and methane (CH 4 ), for example, still volatile hydrocarbons.
  • Plastics for example, consisting only of carbon and hydrogen, pyrolyze under exclusion of air exclusively to lower hydrocarbons.
  • carbon-containing fuel materials can be converted to useful gases with gasification agents, for example carbon with a deficiency of O 2 to CO, then carbon with water (H 2 O) to CO and H 2 , then CH 4 with O 2 to CO.
  • gasification agents for example carbon with a deficiency of O 2 to CO, then carbon with water (H 2 O) to CO and H 2 , then CH 4 with O 2 to CO.
  • the gasification reactions of carbonaceous fuel with H 2 O are endothermic.
  • a natural gasification agent is used in particular air, which may also be enriched with H 2 O, for example as an aerosol or vapor.
  • a gasification agent is understood to mean a pure substance or substance mixture whose addition to the carbonaceous fuel material increases the conversion into useful gases.
  • the gasification of carbonaceous fuel to Nutzgas is predominantly economical only if the fuel is not only readily available or cheap, but the gasification in their energy balance depends solely on the energy content of the fuel.
  • This relates in particular to the use of the useful gas as actual fuel for internal combustion engines, for example for the operation of a gas engine or a gas turbine.
  • the gasification of carbonaceous fuel to Nutzgas then requires a total exothermic running overall process, the energetic itself as long as enough fuel is available.
  • the heat released can also be used, for example, for heating residential buildings, as is the case with combined heat and power in combined heat and power plants (CHP).
  • CHP combined heat and power plants
  • an internal combustion engine is in turn coupled to a generator, which then finally converts mechanical energy into electrical energy.
  • wood is a carbonaceous fuel, like a normal grate on a grid.
  • air is sucked through the grate and the burning wood as a gasifying agent.
  • the upper layers of wood burn only partially and pyrolyze at the same time to Nutzgas, which is sucked off at the upper end of the furnace.
  • Air and natural gas move countercurrently in the opposite direction to the slowly sinking wood.
  • the resulting useful gas has a relatively low temperature of about 100 ° C and contains due to the ongoing drying and pyrolysis of the wood correspondingly much water vapor and organic constituents, which condense on further cooling to an acidic wood tar.
  • the wood tar produced in the countercurrent and DC wood gasification processes is not suitable for internal combustion engines, but damages them due to its adhesive properties.
  • similar high-viscosity residues occur, which are generally referred to as condensate in the present invention.
  • the resulting condensate not only reduces the efficiency with respect to material utilization balance of the gasification reactor, but must be removed from the useful gas by a gas scrubber. This additionally reduces the energy balance of the entire system and additionally requires washing liquid, for example water. Since the condensate is not only corrosive due to its pH, but also toxic and difficult to biodegrade, this results in a disposal problem.
  • fluidized bed gasification reactors in which the fuel is converted into useful gases in an incomplete fluidized bed furnace. In this case, no condensate is generated, since this is also converted to Nutzgasen.
  • gasification in fluidized-bed gasification reactors is restricted to solid fuel materials having a particle size of less than 40 mm with a water content of at least 25% by weight, the particles being suspended by a fluid medium that constantly swirls, for example air. have to. To maintain the fluidized bed, therefore, an external fluid supply with a high flow rate is necessary, which corresponds to an externally supplied work.
  • fluidized-bed gasification reactors can not be operated autothermally, but only allothermally, ie with the supply of external heat energy.
  • the total supply of these two types of energy shall be deducted from the total efficiency of the installation.
  • This gasification technology is only economical for power plants in the power range of 1, 5 to 3 MW, whereby the overall efficiency is only about 30%.
  • a special form of the fluidized-bed gasification reactor is the Winkler generator, in which the fluidized bed can be maintained even better in the entire reactor space by means of ring loops arranged in series around the reactor body.
  • Advantages of the Winkler generator are a homogeneous temperature distribution and better mixing of the particles compared to other fluidized bed gasification reactors.
  • the Winkler reactor is only suitable for the gasification of coal, especially lignite, limited to the smallest possible particle size.
  • a significant improvement of the fluidized bed gasification reactor is provided by the entrained flow gasification reactor in which the carbonaceous
  • Fuel is introduced as dust, slurry or paste as a burner in the gasification room.
  • the gasification processes take place in a cloud of dust.
  • This form of supply requires a corresponding pretreatment of the fuel, especially in biomass as a fuel to be introduced via a pneumatic system in the carburetor and gasified there in a very short time. Even such systems can be operated only with supply of work and heat energy.
  • the supply of heat energy by a continuous ignition with a Zündfackel.
  • the Koppers-Trotzek reactor as a special form of entrained flow gasification reactor is particularly suitable for the gasification of finely ground coal to useful gas.
  • the coal dust is fed in laterally at high speed, so that only a single ignition is needed and the gasification process otherwise autothermal can be performed.
  • operation of the Koppers-Trotzek reactor still requires the supply of work to maintain the flow of air.
  • the gasification processes can not be maintained solely by the supply of fuel.
  • the overall efficiency is limited to a maximum of 30 to 40% by the necessary supply of work to maintain the vortex or flight flow.
  • fluidized bed and entrained flow gasification reactors are limited to the specific nature of the carbonaceous fuel material, in principle, a pretreatment of the respective carbonaceous fuel material is required. Necessary pretreatments of the fuel material also considerably limit the cost-effectiveness of gasification plants, in particular CHP plants.
  • the invention has for its object to improve the efficiency of a gasification reactor for the gasification of carbonaceous fuel to Nutzgasen with respect to Nutzgas- and heat yield and its operational stability by a corresponding operating method.
  • This object is achieved by the combination of features of claim 1 in an inventive manner
  • the back-related claims include some advantageous and partially for themselves inventive developments of the invention.
  • the invention is based on a gasification reactor with a reaction chamber for the gasification of carbonaceous fuel by adding gasification agents to Nutzgasen.
  • the reaction chamber is the carbonaceous fuel.
  • a continuous supply can take place via a reservoir connected to the reaction chamber.
  • the conversion to the Nutzgasen as the sum of all individual pyrolysis and gasification reactions therefore takes place predominantly in the reaction chamber.
  • the gasification reactor according to the invention can also be designed completely as a reaction chamber.
  • composition, amount, pressure, velocity, temperature and / or specific exit pulse of a gasification agent added via control inputs of the reaction chamber are variably controlled according to claim 1 by means of a number of controlled variables determined in the reaction chamber.
  • a variable adjustment of the operation of the respective present states in the reactor is possible and it can be done an optimized gasification of the fuel.
  • Another important feature is the composition, in particular the calorific value of the useful gas used as a controlled variable. This is essentially influenced by the proportion of the water fed to the reaction chamber. By reduction of hydrogen and carbon monoxide are generated from water and carbon, which have a high calorific value. For example, if the calorific value of the useful gas is too low, the supply of water vapor in the gasification agent can be increased.
  • the volume flow of the Nutzgases is used as a control variable. This is also influenced by the proportion of the water fed to the reaction chamber, but in addition also by the total amount of the supplied gasification agent. A higher amount of gasification agent increases namely the gas volume in the reaction chamber and thus also the volume flow at the outlet.
  • the respective pressure in a reservoir for the fuel, in the reaction chamber and / or in a gas outlet is used as a controlled variable.
  • the pressure in the reaction chamber is influenced essentially by the total amount of the gasification agent supplied, but also by the respective distribution of the gasification agent via the various control inputs.
  • the reaction chamber in this case has a plurality of control inputs and composition, amount, pressure, speed, temperature and / or specific exit pulse of the added via the respective control input gasification agent will be controlled at least partially independently of the other control inputs. Consequently, during operation of the gasification reactor, several, ideally every position within the reaction chamber are accessible through these control inputs.
  • Each individual control input thus defines a reaction zone, all reaction zones thereby forming the reaction space which completely fills the reaction chamber. Since the control inputs are at least partially controlled independently of one another, in each reaction zone of the reaction space, the addition of gasification agent with respect to its composition, speed, temperature, pressure and amount as well as with respect to the specific exit pulse is variable over time.
  • this can be realized in that the side walls of the reaction chamber are interspersed with a multiplicity of such control inputs or that a holder with a plurality of recessed control inputs projects into the reaction chamber.
  • the side walls of the reaction chamber are interspersed with a multiplicity of such control inputs or that a holder with a plurality of recessed control inputs projects into the reaction chamber.
  • the combination of both constructive possibilities for the arrangement of the control inputs proves to be advantageous, whereby the accessibility of the entire reaction space is.
  • the nature of the fuel material changes.
  • a coking gradient which decreases vertically from the lower to the upper part of the reaction chamber is formed during the progress of the gasification process. Therefore, in the progressing gasification process in the lower reaction zones for gasification of the resulting pure carbon increased water vapor is supplied together with the hot reactor internal gas.
  • C0 2 can be regarded as a gasification agent itself from 600 ° C itself, since then its equilibrium reaction with carbon according to Boudouard to 23% on the side of CO.
  • the gasification means comprise at least one of the components O 2 or H 2 O, the gasification agent CO 2 being generated during the gasification process itself.
  • the amount of the carbonaceous fuel material supplied to the reaction chamber is also variably controlled on the basis of a number of controlled variables determined in the gasification reactor. This allows a further influencing of the parameters within the reaction chamber by externally controllable variables.
  • a temperature in the reaction chamber is used as a controlled variable.
  • a plurality of temperatures in different areas eg the reaction zones described can be used.
  • composition, amount, pressure, speed, temperature and / or specific exit pulse of the gasification agent added via the respective control input are advantageously controlled by means of the temperature in the reaction chamber at the respective control input as a control variable.
  • the respective temperature substantially influences the type of reactions which occur in the respective zone. Higher temperatures, for example, allow the combustion of carbon residues, while comparatively lower temperatures improve the formation of useful gases.
  • the temperature in the respective reaction zone can be influenced by the admission pressure, temperature and the proportion of the water vapor of the gasification agent supplied at the respective control input. If the pressure and temperature of the gasification agent supplied increase, the temperature in this area also increases, while the increase in the means a reduction in the temperature by heat energy consuming reduction operations.
  • the pressure difference should be used as a control variable via a gas-permeable retention device between the reaction chamber and an ash box of the gasification reactor in an advantageous embodiment.
  • An increase in the pressure difference here indicates a blockage of the retention device with carbon residues. These carbon residues arise in particular at comparatively low temperatures, which in turn are generated by a high water vapor content in the gasification agent. An increase in the pressure difference should therefore be counteracted here by reducing the water vapor content.
  • the composition, moisture, lumpiness and / or dust content of the fuel are used as controlled variables.
  • the respective parameters within the reaction chamber can be optimally adapted to the fuel used.
  • such operated gasification reactor is suitable for a variety of different fuel materials.
  • the inventive method allows an optimal and accelerated reaction of the gasification process with respect to Nutzgasausbeute in its entire time through the regulated, locally varied and the history adapted supply of gasification agent.
  • the formation of condensate is avoided, since the residence time of the hydrocarbons can be made as long as possible by regulating the process, so that the cracking of hydrocarbons (tars) in as small as possible Pieces can be done.
  • the regulation of the process ensures that the temperatures in the flowed through spatial areas are uniformly high so that the cracking reaction of the condensate takes place as quickly as possible.
  • gasification reactor replaces the Winkler generator necessary, extremely energy-consuming preservation of the fluidized bed for optimal and condensate-free gasification of the fuels. Furthermore, a gasification reactor operated according to the invention does not require continuous ignition of the fuel material operated with it, for example by means of an ignition flare.
  • the process according to the invention combines the advantages of fluidized-bed and air-current gasification reactors with those of fixed-bed gasification reactors, whereby only a fraction of external work for supplying the gasification agent and recycling the internal reactor gas must be supplied in comparison to maintaining a fluidized bed or a flow stream. For this external work, a fraction of the generated useful gas is sufficient.
  • the useful gas generated by the method according to the invention can be supplied to an internal combustion engine, which in turn is coupled to a generator. The work necessary to control the reactor is then provided by a fraction of the electrical energy converted by the generator.
  • the performance of the inventively operated reactor depends solely on the chemical energy content of the carbonaceous fuel. Overall, the method provides a stable and completely autothermal operation of the gasification reactor according to the invention with a high overall efficiency, in particular as a subsystem of a CHP.
  • each type and form of carbonaceous fuel material can be used in any state of aggregation for gasification.
  • a DC fixed bed reactor designed according to the invention may additionally have a gas feed device in the reaction chamber.
  • plastic waste and household waste as an example of extremely inhomogeneous mixtures of carbonaceous fuel materials can be gasified with a high overall efficiency in a DC fixed bed reactor according to the invention.
  • the variation of process characteristics is possible. First, it is possible to vary the number of reaction zones.
  • the initially independent control inputs may be controlled to form either a single total reaction zone or a plurality of arbitrarily partitionable partial reaction zones. If, for example, the control inputs are combined into independent independent reaction zones by means of horizontal loops circulating over the reaction chamber, the reaction zones which are independent of one another can be operated in parallel and thus combined to form a larger reaction zone.
  • This variation of the geometry of reaction zones can also be realized by the change, amount and composition of the gasification agent in the radial direction. In this way, inactive, "cold" interior areas are avoided, the entire reaction space is thus activated in terms of process technology, and finally it is possible to vary the respective chemical reaction in the individual reaction zones During operation of the reactor, it is possible to change, change, spatially expand or accelerate the reactions at any point in the reaction space during operation of the reactor.
  • the melting of the solid fuel into readily volatile pyrogas, charcoal, water, higher-chain hydrocarbons, ie a so-called pyrolysis reaction may be mentioned.
  • the aim is to achieve a high heat input with as little air supply as possible. This is done by preheating the gasification agent, by supplying superheated steam and by external preheating of the solid fuel.
  • Switching the zone reaction of pyrolysis in the solid fuel to oxidation in the coal bed occurs when, after filling and during start-up of the reactor, the lower zones are initially filled with solid fuel and pyrogenic be operated table. After the outgassing of the volatile pyrogase, the zone is then switched to oxidative or reductive operation.
  • the gas phase reaction can take place both oxidatively in the solid fuel-free and carbon-free regions produced by intermediate bottoms.
  • the gas phase reaction can be proportionally reduced by greatly increasing the velocity of the gasifying agents by supplying them by means of controllable nozzles without increasing the mass flow, as long as the stream, so-called “sharp jet", strikes the coal bed located behind the cavity.
  • the reaction rate in the reaction zones can be varied.
  • the gasification agent supply in the coal bed is increased.
  • the reduction in the supply of gasification equals a reduction in its geometry and / or a reduction in the reaction rate in this zone.
  • the increase in the supply of gasification is associated with an increase in their geometry and / or with an increase in the reaction rates of the reactions occurring therein, so that the carbon is degraded oxidatively or reductively.
  • the pyrozone is geometrically reduced or reduced in intensity, while the reaction zones for coal mining increased, or increased in intensity.
  • the amount, composition, temperature or pressure of the gasifying agent in the reaction zones can be varied.
  • a variation of the amount of the gasifying agent essentially affects the Reaction speed and partly on the nature of the reaction.
  • the composition of the gasifying agent also affects the nature of the reaction.
  • the temperature variation causes a change in the reaction rate.
  • a variation of the pressure in turn affects the speed and amount of the gasifying agent.
  • a - as far as possible - decoupling of all influencing variables is achieved via adjustable nozzles.
  • Fig. 2 is a gasification reactor with central hedgehog-like supply line
  • Fig. 3 is a schematic representation of the control and control variables with their mutual influence.
  • the embodiment in Fig. 1 relates to a gasification reactor 1, which is designed in particular for the gasification of solid carbonaceous fuel.
  • the gasification reactor 1 is designed as a fixed bed reactor according to the DC principle.
  • the gasification reactor according to FIG. 1 is suitable for carrying out the process according to the invention.
  • the gasification reactor 1 has a permeable intermediate bottom 2, which divides the gasification reactor 1 into an upper reservoir 3 and into a lower reaction chamber 4. Another permeable intermediate bottom 5 separates the reaction chamber 4 from the ash box 6 as the lowest subspace of the entire gasification reactor 1 from.
  • a gas-permeable retention device 7 in the form of a grate between the reaction chamber 4 and the ash box 6 ensures that the fuel remains in the reaction chamber 4.
  • a gas outlet 8 is attached. Via the reservoir 3, the carbonaceous, solid fuel is fed to the reaction chamber 4, the useful gas is discharged via the gas outlet 8. After filling reservoir 3 and reacting Onshunt 4 with the carbonaceous solid fuel, the gasification reactor is ignited once in the lower reaction zones and then started by air.
  • the side wall 9 of the reaction chamber 4 of the gasification reactor 1 is interspersed with a plurality of control inputs 10 in such a way that in the operation of the gasification reactor each position within the reaction chamber 4 is accessible through the control inputs 10.
  • the control inputs 10 are horizontally over the reaction chamber circulating ring lines 11 to flat, but summarized independent reaction zones. By the respective independent ring lines 11 the addition of gasification agent or the return of the reactor internal gas with respect to composition, temperature and pressure and thus quantity is then controlled via the combined via web connections 12 control inputs 10.
  • the control is individual for each area reaction zone.
  • the reservoir 3 of the gasification reactor 1 has a larger diameter and a larger volume than the reaction chamber 4, wherein the permeability of the intermediate bottom 2 is given by an opening with a diameter which is smaller than that of the reservoir 3 and the reaction chamber 4, but greater than the opening of the intermediate bottom 5 is.
  • the reactor with its reservoir 3, the reaction chamber 4 and its ash box 6 are cylindrical, the openings of the shelves 2 and 5 are circular.
  • This embodiment of the gasification reactor 1 allows its embedding in a vollum passerde insulation, whereby the reactor efficiency is further increased.
  • the gasification reactor 1 is designed to withstand deflagration of the gasification products as well as the fuel.
  • the gasification reactor 1 according to FIG. 2 likewise has an upper reservoir 3 and a permeable intermediate bottom 2.
  • the reaction chamber 4 is charged by nozzle-shaped nozzle entrances 13 arranged in the form of a nozzle.
  • the nozzle entrances 13 form the control inputs 10 of the embodiment in FIG.
  • the gasification reactor 1 according to Hg. 2 corresponds in its construction to that in FIG. 1.
  • Control parameters which can be directly influenced by the control are here the total amount of gasification agent 20, the admission pressure 22 of the gasification agent at the nozzle or control inputs 10, 13, the respective distribution 24 of the gasification agent to the individual nozzle or control inputs 0, 3, that of a spatial distribution corresponds to the temperature 26 of the gasifying agent and the water vapor content 28 in the gasification agent.
  • controlled variables are detected: the flow 30 of the generated Nutzgases, the differential pressure 32 on the lower shelf 5, the chemical Nutzgaszusammen substance 34, the pressure 36 in the reaction chamber 4, the temperature 38 in the reaction chamber 4 at the respective control input 10 and the type of reactions occurring 40.
  • the latter can typically not be measured directly but can only be determined as a derived controlled variable.
  • the volume flow 30 of the useful gas is influenced by the total amount of gasification agent 20, since an increased supply of gaseous gasification agent via a gain factor Nutzgases increased. Furthermore, this is influenced by the water vapor content 28 in the gasification agent, since introduced water vapor is split reductively and thus causes an increase in the volume and thus the volume flow 30 of the exiting useful gas.
  • the differential pressure 32 across the intermediate bottom 5, which is permeable to gas, is essentially an indicator of an increased deposition of carbon residues blocking the gas throughput of the intermediate bottom 5. Carbon remains at lower temperatures when the carbon is not burned. This is particularly the case with a high water vapor content 28. Thus, the water vapor fraction 28 influences the differential pressure 32. If the distribution 24 of the supplied gasification agent is changed such that more gasification agent is introduced at control inputs 10 in the region of the intermediate bottom 5 and the temperature here increases, the accumulated carbon is burned and the differential pressure 32 decreases.
  • the gas composition of the useful gas 34 depends essentially on the proportion of the water vapor 28. A higher amount of water vapor leads to a higher proportion of hydrogen in the useful gas.
  • the pressure 36 in the reactor chamber 4 should not deviate too far from the ambient pressure. It is essentially influenced by the total quantity 20 of the gasification agent supplied, and also by the spatial distribution 24 of the gasification agent.
  • the temperatures 38 in the various regions of the reactor chamber 4 are influenced above all by the spatial distribution 24 of the gasification agent, but also by admission pressure 22 and temperature 24 of the gasification agent, as well as the water vapor fraction 28 in the gasification agent, as explained above.
  • the type of chemical reactions occurring 40 is also, as already explained, essentially determined by the water vapor content 28 in the gasification agent, and also by the temperature of the introduced gasification agent.
  • the control according to the inventive method now takes into account the control variables recorded in the reactor 1 and accordingly sets the control variables for optimized gasification.
  • the gasification reactor 1, operated with a method under control of the variables described in this embodiment is designed for a CHP, so for the heat and power.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Mechanical Engineering (AREA)
  • Processing Of Solid Wastes (AREA)

Abstract

L'invention concerne un procédé de fonctionnement d'un réacteur de gazéification (1) comprenant une chambre de réaction (4) destinée à la gazéification autothermique et/ou allothermique d'une matière combustible carbonée en gaz utiles, ledit procédé devant améliorer le rendement du réacteur de gazéification destiné à la gazéification d'une matière combustible carbonée en gaz utiles, en termes de rendement en gaz utiles et de rendement thermique tout comme de stabilité de fonctionnement. A cet effet, composition, quantité, pression, vitesse, température et/ou impulsion de sortie spécifique d'un agent de gazéification ajouté à la chambre de réaction (4) par l'intermédiaire d'entrées de régulation (10) sont commandées de manière variable à l'aide d'un certain nombre de grandeurs de réglage déterminées dans la chambre de réaction (4); la composition (34) du gaz utile et/ou du flux volumique (30) du gaz utile et/ou la pression (36) respective dans un réservoir (3) destiné à la matière combustible, dans la chambre de réaction (4) et/ou dans la sortie de gaz (8) étant utilisées comme grandeurs de régulation (30, 32, 34, 36, 38, 40).
EP12783523.9A 2011-10-28 2012-10-26 Procédé de fonctionnement d'un réacteur à gazéification Withdrawn EP2771437A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102011117140A DE102011117140A1 (de) 2011-10-28 2011-10-28 Verfahren zum Betreiben eines Vergasungsreaktors
PCT/EP2012/004503 WO2013060474A1 (fr) 2011-10-28 2012-10-26 Procédé de fonctionnement d'un réacteur à gazéification

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EP2771437A1 true EP2771437A1 (fr) 2014-09-03

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DE202012008777U1 (de) * 2012-09-13 2015-10-06 Big Dutchman International Gmbh Vorrichtung zur Erzeugung von Brenngas aus einem festen Brennstoff
CN106753578A (zh) * 2016-12-16 2017-05-31 四川雷鸣环保装备有限公司 脉冲式循环流化床气化炉及使用该气化炉的气化系统及方法

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US5607487A (en) * 1993-03-17 1997-03-04 Taylor; Leland T. Bottom feed - updraft gasification system
DE102004020919B4 (de) * 2004-04-28 2009-12-31 Kbi International Ltd. Reaktor zur thermischen Abfallbehandlung mit Eindüsungsmitteln
WO2007002847A2 (fr) * 2005-06-28 2007-01-04 Community Power Corporation Procede et appareil pour filtre autonettoyant
AP2008004698A0 (en) * 2006-06-05 2008-12-31 Plascoenergy Ip Holdings S L A gasifier comprising vertically successive processing regions
FR2914314B1 (fr) 2007-03-26 2011-04-08 Litelis Procede et installation pour la gazeification a puissance variable de matieres combustibles.
US8105401B2 (en) * 2007-07-10 2012-01-31 Refill Energy, Inc. Parallel path, downdraft gasifier apparatus and method

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DE102011117140A1 (de) 2013-05-02

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