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WO2013060457A1 - Procédé d'élimination automatique d'un excédent de carbone dans un réacteur de gazéification - Google Patents

Procédé d'élimination automatique d'un excédent de carbone dans un réacteur de gazéification Download PDF

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Publication number
WO2013060457A1
WO2013060457A1 PCT/EP2012/004458 EP2012004458W WO2013060457A1 WO 2013060457 A1 WO2013060457 A1 WO 2013060457A1 EP 2012004458 W EP2012004458 W EP 2012004458W WO 2013060457 A1 WO2013060457 A1 WO 2013060457A1
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WIPO (PCT)
Prior art keywords
gasification
reaction chamber
carbon
reactor
excess
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.)
Ceased
Application number
PCT/EP2012/004458
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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
Priority to EP12786817.2A priority Critical patent/EP2771438A1/fr
Publication of WO2013060457A1 publication Critical patent/WO2013060457A1/fr
Anticipated expiration legal-status Critical
Ceased 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
    • C10J3/72—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
    • C10J3/34—Grates; Mechanical ash-removing devices
    • 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
    • C10J2300/092—Wood, cellulose
    • 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
    • C10J2300/0973—Water
    • C10J2300/0976—Water as steam
    • 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
    • C10J2300/1625—Integration of gasification processes with another plant or parts within the plant with solids treatment
    • C10J2300/1637—Char combustion

Definitions

  • the invention relates to a method for the automatic removal of a carbon excess in a gasification reactor with a reaction chamber for the autothermal and / or allothermal gasification of carbonaceous fuel to Nutzgasen.
  • 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, fossil fuels, and synthetic-organic materials, especially carbon-containing plastics.
  • biomass is generally understood to mean any carbonaceous substance derived directly or indirectly from physiological processes of living organisms,
  • CONFIRMATION COPY especially from plant photosynthesis, is not deprived of the natural carbon cycle and can be exothermally converted by organisms to CO2.
  • 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 which consist for example only of carbon and hydrogen, pyrolyzed under exclusion of air exclusively to lower hydrocarbons.
  • Carbon monoxide (CO), hydrogen (H 2 ) and methane (CH 4 ) and volatile hydrocarbons are flammable, are ideally suited as fuels for internal combustion engines, are important starting materials for many chemical manufacturing processes and are thus valuable. full useful gases.
  • Methane (CH 4 ) and pure carbon, for example in the form of mineral graphite or synthetic coke, are not or no longer pyrolysable.
  • carbon-containing fuels can be converted to useful gases with gasifiers, 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.
  • gasifiers 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 as a surplus of carbon in 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 limited to solid fuels having a particle size of less than 40 mm with a water content of at least 25% by weight, the particles having to be suspended by a fluid fluid that constantly swirls, for example air. 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 intake of these two types of energy is deduct the degree of the plant. 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 at high speed, so that only a single ignition is needed and the gasification process can otherwise be performed autothermally.
  • 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. In all versions of these reactor types, 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 supply of external work is limited only to that of the carbonaceous fuel and the gasifier, maintaining optimal conditions for the pyrolysis as well as gasification reactions is generally more difficult.
  • the invention is therefore based on the object to provide a method which allows a particularly high efficiency and very high operational stability with lower demands on the fuel used in the operation of a gasification reactor.
  • This object is achieved by the feature combination of claim 1 in an inventive manner.
  • the dependent claims include in part advantageous and in part self-inventive developments of the invention.
  • the invention is based on the idea that a particularly high degree of efficiency as well as a particularly high operational stability would be achievable if an automatic removal of carbon excesses, which could lead to clogging of the reactor, would be possible.
  • the invention is based on a gasification reactor with a reaction chamber for the gasification of carbonaceous fuel by the addition of gasification agents to Nutzgasen based.
  • the reaction chamber In 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 can also be designed completely as a reaction chamber.
  • An essential feature of the invention according to claim in the exceeding of a predetermined, characteristic of the amount of excess carbon in the reaction chamber composition, amount, pressure, velocity, temperature and / or specific exit pulse of the reaction chamber added gasification agent such that combustion of Carbon excess is increased.
  • the gasification reactor is not operated in a certain operating state like all known reactors, but upon detection of excessive carbon excess in the reaction chamber, the reaction conditions in the chamber are changed such that this carbon excess degraded, ie burned. The reactor thus switches from a gasification to a carbon combustion mode.
  • the change in the fall below a second predetermined, characteristic of the amount of carbon excess in the reaction chamber value is reversed. That is, as soon as it is detected that a sufficient amount of excess carbon is burned and the carbon amount has no more critical value, is switched back to the "normal" operating state of the reactor, thereby ensuring that the operating state for the combustion of excess carbon, temporarily a lower Efficiency, as the normal operating state designed for optimum gasification, is maintained only for a minimal time, but just long enough to sufficiently ensure removal of carbon.
  • the determination of excessive carbon surplus in the reactor is made on the basis of a value characteristic of the amount of carbon surplus.
  • a variety of values can be used.
  • a predetermined pressure difference across a gas-permeable retention device between the reaction chamber and an ash box of the gasification reactor is used as such a value.
  • a carbon excess will preferentially deposit on such a retainer.
  • the gas permeability of the retaining device is reduced, and the useful gas produced in the reaction chamber can thus escape more poorly.
  • This increases the pressure difference across the retaining device, which is relatively easy to detect with corresponding pressure sensor. This is a simple yet reliable measure of the amount of excess carbon in the reaction chamber.
  • the main accumulation of excess carbon in the retention device described allows a further optimization of the method.
  • the operating parameters are changed in such a way that the carbon is gasified here. This also makes it possible to maintain the gasification reaction under normal operating conditions in other areas where the accumulation of carbon is less high.
  • the combustion of carbon can be achieved by advantageously increasing the amount of added gasification agent.
  • a larger amount of oxygen allows the oxidation of the carbon.
  • the water vapor content in the gasification agent is reduced. This reduces the energy-consuming reduction reaction, increases the temperature and thus promotes combustion of carbon.
  • the method is embedded in a higher-level control, wherein the reaction chamber thereby (preferably has multiple) control inputs and composition, amount, pressure, speed, temperature and / or specific exit pulse of the gasification agent are variably controlled by a number of determined in the reaction chamber controlled variables.
  • the gasification agent added via the respective control input is advantageously at least partially controlled independently of the respective 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.
  • 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 combination of both constructive ways for the arrangement of the control inputs proves to be advantageous, whereby the accessibility of the entire reaction space is guaranteed.
  • the nature of the fuel material changes.
  • a gas phase decreasing from the lower to the upper part of the reaction chamber is formed in the course of the gasification process. 8 kohlungsgradient off. 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 agents comprise at least one of the components O 2 or H 2 O, wherein the gasification agent CO 2 is generated during the gasification process itself.
  • the regulation described now makes it possible not to achieve the combustion of carbon by setting predetermined combustion parameters, but by prescribing one or more setpoint values for the respective control variables. As a result, the higher-level control is maintained and the operation can be optimally maintained even in the combustion operating state.
  • the setpoint temperature is changed as a controlled variable.
  • Such a change is answered by the regulation accordingly with an increase in the amount of combustion agent and the reduction of the water vapor content, since these measures increase the temperature.
  • the embedding of the method described in a higher-level control also allows in a particularly simple manner, the maintenance of the gasification in areas of the reaction chamber with lower carbon deposits.
  • the target value of the temperature is reduced as a controlled variable. As a result, the gasification is continued here, while in the region of the retaining device, the carbon combustion takes place.
  • the amount of fuel supplied to the reaction chamber is reduced.
  • the fuel content is temporarily reduced in the reaction chamber, since the gasification initially continues. This promotes easier combustion of carbon.
  • the inventive method allows optimal and accelerated removal of carbon excesses in the reaction chamber by the controlled and the course adapted switching to a combustion-promoting operating state.
  • the controlled combustion of carbon by temporally and locally individually metered addition of gasification agents in the gasification reactor on which the invention is based replaces the extremely energy-conserving maintenance of the fluidized bed required for the Winkler generator for optimal and condensate-free gasification of the fuels.
  • 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.
  • the method according to the invention is particularly advantageous over all embodiments of vortex and entrained flow gasification reactors in that 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.
  • Much finer-grained wood chips may also be used instead of the traditionally used coarse-grained chips, since the blockage of the reactor caused by the use of the cheaper fine-grained fuel can be eliminated by the described method.
  • Fig. 3 is a schematic representation of the control and control variables in the case of involvement in a scheme with their mutual influence and
  • FIG. 4 is a schematic representation of the different operating states for gasification and carbon combustion.
  • 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 reaction chamber 4 with the carbonaceous, solid fuel material, the gasification reactor in the lower reaction zones is ignited once and then started up by supplying 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 outg
  • the gasification reactor 1 allows its embedding in a fully enclosing 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.
  • the nozzle inlets 13 form the control inputs 10 of the gasification reactor 1.
  • the gasification reactor 1 according to FIG. 2 corresponds in its construction to that in FIG. 1.
  • Control parameters that 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 10, 13, 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.
  • FIG. 3 now shows the respective relationships between control variables and control variables, as required in the method according to the invention when incorporated into a control: 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 increases the volume flow through the entire reactor 1. Furthermore, it is influenced by the water vapor fraction 28 in the gasification agent, since introduced water vapor is hydrolytically split 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 retention device 7, which is permeable to gas, is essentially an indicator of increased deposition of carbon residues blocking the gas flow rate of the retention device 7. 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 at control inputs 10 in the region of the retaining device 7 more gasification agent is introduced and the temperature increases here, Thus, the accumulated carbon is burned and the differential pressure 32 decreases. This will be explained in more detail below.
  • 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 described control is active during the operation of the reactor 1. If required, a targeted combustion of carbon is now initiated when a too high differential pressure 32 is detected, a limit being specified for this purpose.
  • the goal here is a temperature increase in the area of the retention device 7. This can be achieved either by specifying appropriate temperature setpoints with active control, or by direct control of the supplied gasification agent. The resulting temperature profile is shown in FIG. 4.
  • the 4 shows a characteristic of the two operating conditions temperature profile within the reaction chamber 4.
  • the vertical axis of the reaction chamber is plotted on the abscissa, the upper area is left with the fuel supply to the left, while the right is the lower area with the retaining device 7.
  • the lines 42 each indicate the location of the independently controllable control inputs 10, the line 44 marks the rough distinction in more (right) and less (left) areas affected by carbon surplus deposits.
  • Line 46 indicates the maximum temperature distribution to be maintained by the control and line 48 the minimum thereof to ensure smooth operation of the reactor 1. Within the limits 46 and 48, the temperature is now adapted to the two operating states.
  • Temperature line 50 shows the temperature distribution during normal operation. In the lower part of the temperature is the lowest, to ensure an optimal composition of the Nutzgases. In the upper area the temperature is comparatively high. In the lower area, but here it can be a Excess carbon come, which deposits on the restraint device 7. This is determined in the form of an increase in the pressure difference 32.
  • the system is switched to the freewheeling operating state.
  • the resulting temperature distribution represents temperature line 52.
  • the temperature is now lower, while in the lower region, i. at the restraint device 7 almost increases to the given by line 46 maximum.
  • carbon is oxidized here.
  • the retaining device 7 is again free of carbon, which is determined by falling below a predetermined limit value of the pressure difference 32, the temperature line 50 is switched back to the normal state.
  • the controlled switching to the freebearing operating state according to the method according to the invention taking into account the control which takes into account the control variables recorded in the reactor 1, sets the control variables as required for optimized combustion of excess carbon.
  • 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. Through thermal integration of all subsystem units of the entire system, combined heat and power generation achieves an overall efficiency of> 85%.

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Abstract

L'invention concerne un procédé d'élimination automatique d'un excédent de carbone dans un réacteur de gazéification (1) comprenant une chambre de réaction (4) pour la gazéification autothermique et/ou allothermique d'une matière combustible carbonée en gaz utiles. Ce procédé doit permettre un rendement particulièrement élevé et une stabilité de fonctionnement particulièrement élevée pour de faibles exigences en termes de combustible utilisé pour le fonctionnement d'un réacteur de gazéification. A cet effet, lors du dépassement d'une valeur prédéfinie, caractéristique de la quantité d'excédent de carbone dans la chambre de réaction (4), on modifie la composition, la quantité, la pression, la vitesse, la température et/ou l'impulsion de sortie spécifique d'un agent de gazéification ajouté à la chambre de réaction (4) de manière à augmenter une combustion de l'excédent de carbone.
PCT/EP2012/004458 2011-10-28 2012-10-25 Procédé d'élimination automatique d'un excédent de carbone dans un réacteur de gazéification Ceased WO2013060457A1 (fr)

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DE102011117141A DE102011117141A1 (de) 2011-10-28 2011-10-28 Verfahren zur automatischen Entfernung eines Kohlenstoffüberschusses in einem Vergasungsreaktor

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DE102011119386A1 (de) 2011-11-25 2013-05-29 Ligento green power GmbH Verfahren zum An- und Abfahren einer Vergasungsanlage

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WO2007002844A2 (fr) * 2005-06-28 2007-01-04 Community Power Corporation Procede et dispositif modulaire automatise de production d'energie utilisant de la biomasse
US20070289216A1 (en) * 2006-06-05 2007-12-20 Plasco Energy Group Inc. Gasifier comprising vertically successive processing regions
US20100107494A1 (en) 2007-03-26 2010-05-06 Litelis Method and installation for variable power gasification of combustible materials

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DE3924626A1 (de) * 1989-07-26 1991-01-31 Forschungszentrum Juelich Gmbh Vergasungsreaktor fuer brennbare feststoffe

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US20020046686A1 (en) * 2000-10-20 2002-04-25 Malahat Systems Corporation Gasifier
WO2007002844A2 (fr) * 2005-06-28 2007-01-04 Community Power Corporation Procede et dispositif modulaire automatise de production d'energie utilisant de la biomasse
US20070289216A1 (en) * 2006-06-05 2007-12-20 Plasco Energy Group Inc. Gasifier comprising vertically successive processing regions
US20100107494A1 (en) 2007-03-26 2010-05-06 Litelis Method and installation for variable power gasification of combustible materials

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