EP2771436A1

EP2771436A1 - Gasification reactor for carbon-containing fuel

Info

Publication number: EP2771436A1
Application number: EP12784458.7A
Authority: EP
Inventors: Martin ZUCKERMAIER; Thomas Tschaftary
Original assignee: Ligento Green Power GmbH
Current assignee: LIGENTO GREEN POWER GMBH
Priority date: 2011-10-28
Filing date: 2012-10-26
Publication date: 2014-09-03
Also published as: DE102011117142A1; WO2013060473A1

Abstract

There is specified a gasification reactor (1) having a reaction chamber (4) for the autothermal gasification of carbon-containing fuel to form useful gases, wherein the reaction chamber has a plurality of control inputs (10) which are at least partially independent of one another. The gasification process is controlled by means of the recirculation of the gas within the reactor and/or by means of the addition of gasification agents via the control inputs (10).

Description

description

Gasification reactor for carbonaceous fuel

The invention relates to a gasification reactor for the autothermal gasification of carbonaceous fuel to Nutzgasen. It further relates to a method for operating such a gasification reactor, a method for the automatic removal of condensate from such a gasification reactor and method for its start-up and emergency shutdown.

definitions

In the present invention, 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.

In the present invention, 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.

In the present invention, 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. In this sense, the carbonaceous fuel includes, in particular, biomass, fossil fuels, and synthetic-organic materials, especially carbon-containing plastics. In the present invention, biomass is generally understood to mean any carbonaceous substance derived directly or indirectly from physiological processes of living organisms,

CONFIRMATION COPY in particular from plant photosynthesis, is not deprived of the natural carbon cycle and can be exothermally converted by organisms to CO ₂ . Examples of biomass are fermentation residues, wood, leaves, hay, straw, paper, cardboard, compost, faeces and sewage sludge.

In the present invention, 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. Examples of 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. Thus, 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.

Technical background

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. In particular, in 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.

However, 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. However, the gasification reactions of carbonaceous fuel with H ₂ O are endothermic. As 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. In the present invention, therefore, 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. In addition, 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). In a CHP, an internal combustion engine is in turn coupled to a generator, which then finally converts mechanical energy into electrical energy.

The combustion of carbonaceous fuel with O ₂ to CO, however, is so weakly exothermic that the energy released is not sufficient to sustain simultaneously ongoing pyrolysis and / or gasification reactions with H ₂ O permanently. The energy required for the entire gasification process must therefore be replaced by the highly exothermic combustion reaction of carbon monoxide. fuel with 0 ₂ to C0 _{2 are} applied. The highest possible efficiency in terms of Nutzgas- and heat yield of such an autothermal gasification is achieved at an optimum, in which the extent of combustion to CO ₂ just sufficient to provide the necessary energy contribution for pyrolysis and gasification reactions. This optimum in terms of incomplete combustion depends on the composition and nature of the fuel, the supply or optimal metering of the gasification agent, the nature and isolation of the gasification reactor and thus summarized by the entire reaction. Here, the change in the fuel during the entire gasification process is also taken into account or not negligible.

In the classic fixed-bed gasification reactor, wood is a carbonaceous fuel, like a normal grate on a grid. As a countercurrent process, 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.

In the co-current method for wood gasification, air is fed as a gasifying agent directly above the grid directly into the hot gasification reaction zone of the fixed-bed gasification reactor and sucked under the grate. The internal reactor gas and the useful gas and air move in the same direction in the area of the grid, ie in direct current. The temperature of the reactor internal gas or useful gas is much higher here than in the countercurrent process. The useful gas as end product from the reactor internal gas contains significantly less wood tar, wherein the wood tar produced in the DC process has a basic pH.

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. Also in the gasification of other carbonaceous fuels, 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. In US 2010/0107494 A1 a fixed-bed gasifier for biomass is proposed with a successive fuel supply, which promises a higher efficiency in terms of fuel turnover, but does not eliminate the formation of condensate or the resulting condensate can not continue to use in the gasification process.

One approach to the gasification of carbonaceous solid fuels is to use 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. However, 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. Furthermore, 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. However, 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. Here, 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. Here, 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. However, operation of the Koppers-Trotzek reactor still requires the supply of work to maintain the flow of air. Both in the various embodiments of the fluidized bed gasification reactor and those of the entrained flow gasification reactor, 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. According to the prior art fixed-bed gasification reactors with cocurrent or countercurrent principle, 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. Although in fixed-bed gasification reactors compared to the fluidized bed and entrained-flow gasification reactors 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. In fixed bed gasification reactors with a DC or countercurrent principle, the definition of a given fuel quality and piece size, for example, to so-called G50 wood chips, particularly disadvantageous. Deviations from this, especially in terms of piece quality, water content and dust content, cause varying pressure and temperature conditions. Such deviations then require, for example, an excessive supply of air as a gasification agent. This leads to a strong dilution of the Nutzgas by atmospheric nitrogen and water vapor and an increased formation of entrained condensate. Quality and yield of the useful gas are then reduced so much that a costly gas scrubbing must be carried out prior to its utilization. Increased formation of condensate not only significantly lowers the overall efficiency of the plant, but also leads to blockages in the reactor, which can lead to complete failure of the entire plant. In addition, the purification of fixed bed gasification reactors of condensate is very expensive. Task and solution

The invention has for its object to constructively improve the efficiency of a gasification reactor for the gasification of carbonaceous fuel to Nutzgasen with respect to Nutzgas- and heat yield. 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 a gasification reactor with a reaction chamber for the gasification of carbonaceous fuel by adding gasification agents to Nutzgasen. In the reaction chamber is the carbonaceous fuel. In the case of solid fuel materials, 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.

As an essential feature of the invention according to claim 1, the reaction chamber of the gasification reactor on a plurality of at least partially independent control inputs such that the gasification of carbonaceous fuel is controlled by the return of the reactor internal gas and / or by the addition of varying gasification agents through the control inputs. In operation of the gasification reactor, therefore, any position within the reaction chamber is 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.

In terms of design, this is realized by protruding into the reaction chamber a holder with a large number of recessed control inputs. Depending on the predominant nature of the carbonaceous fuel material in interaction with the geometry of the reaction chamber, in particular if the Diameter of the reaction chamber is greater than their height, this arrangement of the control inputs proves to be advantageous, whereby the accessibility of the entire reaction space is ensured. In addition, advantageously, the side walls of the reaction chamber may be interspersed with a plurality of such control inputs or a combination of both constructive options may be provided.

The design of the gasification reactor according to the invention can be optimized in that in relation to the size of the reaction chamber as high a variety of control inputs is thereby realized by the control inputs are designed to be as small as possible, so the reaction space is divided into as many reaction zones. In this way, a particularly advantageous fine adjustment of the gasification process is achieved with respect to optimum heat and Nutzgasausbeute and influencing the running in the reaction chamber thermochemical processes in particular their nature and intensity is achieved.

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.

Throughout the gasification process, the nature of the fuel material changes. In particular, in the gasification of solid, carbonaceous fuel materials in a DC fixed-bed gasification reactor constructed according to the invention, 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. Here, CO2 can even be considered as a gasification agent from 600 ° C, because then whose equilibrium reaction with carbon according to Boudouard is 23% on the side of CO. In summary, therefore, the gasification means comprise at least one of the components O ₂ or H2O, the gasification agent CO2 being generated during the gasification process itself.

Since the gasification process of solid, carbonaceous fuel materials in accordance with the invention carried out DC fixed bed gasification reactors is determined by a predominantly vertically extending reaction gradient, a structural simplification is possible. This constructive simplification is that the control inputs are thus combined horizontally into two-dimensional, but independent, reaction zones by being connected horizontally by ring lines, which in turn circulate the gasification reactor or the reaction chamber. Here, in turn, in each planar reaction zone of the reaction chamber, the addition of gasification agent or the return of the reactor internal gas with respect to composition, temperature and pressure and thus quantity variable over time.

The embodiments of the reactor and / or its reaction chamber may also be adapted to the predominant nature of the carbonaceous fuel. With varying consistency and changing state of matter of the carbonaceous fuel material, the embodiments are based only on structural expediency, for example in the embodiment as polygons or cylinders.

In summary, the gasification reactor according to the invention allows an optimal and accelerated reaction of the gasification process with respect to Nutzgasausbeute in its entire time through the regulated and the course adapted supply of gasification agent than by the simultaneous circulation of the reactor internal gas. Even with the use of solid, carbonaceous fuel materials, such as biomass, the formation of condensate is avoided, since the residence time of the hydrocarbons can be made as long as possible by controlling the process, so that the cracking of the hydrocarbons (tars) in smallest possible pieces can be done. Furthermore, the regulation of the process ensures that the temperatures in the flowed through spatial areas are uniformly high so that the cracking reaction proceeds as quickly as possible.

The compact nature of the gasification reactor according to the invention, in particular of its reaction chamber, ensures a nearly lossless, controllable Nutzgasabfuhr by a device for gas outlet. The compact nature also allows the gasification reactor of the invention to be designed with a heat exchange device. In particular, in the case of a completely enclosing thermal insulation of the reactor, heat arising during the gasification process can again be fed back to the gasification process for increasing the useful gas yield by reducing the nitrogen input and its excess content for further use, in particular in one

CHP, be dissipated.

The temporally and locally individually metered addition of gasification agents in the gasification reactor on which the invention is based replaces the extremely energy-consuming maintenance of the fluidized bed required for the Winkler generator for optimal and condensate-free gasification of the fuels. Furthermore, the gasification reactor on which the invention is based does not require continuous ignition of the fuel material operated with it, for example by means of an ignition torch.

The gasification reactor according to the invention combines the advantages of turbulence and entrained flow 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 the preservation of a fluidized bed or a flow stream. For this external work, a fraction of the generated useful gas is sufficient. The useful gas generated in the gasification reactor according to the invention can be supplied to an internal combustion engine, which in turn is coupled to a generator. The work required to control the reactor is then provided by a fraction of the electrical energy converted by the generator. The performance of the inventive reactor exclusively from the chemical energy content of the carbonaceous fuel from. The design-related advantages afford overall a stable and fully autothermal operation of the gasification reactor according to the invention with a high overall efficiency, in particular as a subsystem of a CHP.

Finally, the gasification reactor according to the invention, particularly in one embodiment as a DC fixed bed reactor, compared to all versions of vortex and entrained flow gasification reactors characterized particularly advantageous that any type and form of carbonaceous fuel in any state of aggregation for gasification can be used. For example, a DC fixed bed reactor designed according to the invention may additionally have a gas feed device in the reaction chamber. Also, 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.

During the operation of the inventive gasification reactor, the variation of procedural features 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 activated in this way in terms of process technology, and finally it is possible to determine the respective chemical reaction in the individual reaction zones. action zones to vary. By changing the reaction taking place in the respective reaction zone, the stratification or the sequence of the reaction zones can be changed during operation. Thus, there is the possibility of changing the reactions during operation of the reactor at any point in the reaction space, to change, to expand spatially or to accelerate.

By way of example, 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 startup of the reactor, the lower zones are first filled with solid fuel and operated pyro- lytically. 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.

Furthermore, it is possible to vary predominantly with oxidation or predominantly with reduction in the coal bed. It is also possible to realize oxidation and reduction simultaneously in the same volume of space in the coal bed. It is also possible to operate oxidation and reduction alternately in the same volume of space in the coal bed. This is done by feeding a zone of air with release of heat. Subsequently, the same zone is charged with water vapor and thus generates a water gas reaction while consuming heat. The change of both reactions occurs intermittently during operation.

Finally, the reaction rate in the reaction zones can be varied. For example, in pyrolysis, by reducing the gasification agent supply, the pyrolysis reaction is stopped and greatly reduced. At the same time, 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. Finally, 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 has an effect on the reaction rate and partly also 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.

The invention will be explained in more detail with reference to two embodiments with reference to the drawing figures. Show it:

Fig. 1 is a gasification reactor with loops and

Fig. 2 is a gasification reactor with central hedgehog-like supply line.

Identical parts are always provided with the same reference numerals. The embodiment in Fig. 1 relates to a gasification reactor 1, which is designed in particular for the gasification of solid carbonaceous fuel. For this purpose, the gasification reactor 1 is designed as a fixed bed reactor according to the DC principle.

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. At the ash box 6, 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 gasification reactor operates as a furnace in over-stoichiometric operation and is thereby brought to operating temperature together with the other system components. Subsequently, the gasification reactor is brought by further addition of fuel or by reducing the air supply in the substoichiometric gasification operation. This operation prevents the escape of unburned gas in the warm-up phase through the chimney or flaring through a special torch. Advantageously, the switchability of the gasification reactor from substoichiometric to superstoichiometric operation or from superstoichiometric to substoichiometric operation can also be used to perform maintenance work on a connected combined heat and power plant or to cover a heat requirement without electricity generation. Furthermore, the gasification reactor and the connected components for rapid shutdown can be completely separated from the outside air. be separated so that the processes in the reactor come to succumb quickly and takes place to the escape of unburned gas in the chimney.

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 vollumschließende insulation, whereby the reactor efficiency is further increased. Regarding the stability in its construction, 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. Incidentally, the gasification reactor 1 according to FIG. 2 corresponds in its construction to that in FIG. 1.

The gasification reactor 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> 90%.

LIST OF REFERENCE NUMBERS

1 gasification reactor

2 intermediate floor

3 reservoir

4 reaction chamber

5 intermediate bottom

6 ash box

7 restraint device

8 gas outlet

9 side wall

10 control input

11 ring line

12 bridge connection

Claims

claims

1. gasification reactor (1) with a reaction chamber (4) for the autothermal and / or allothermal gasification of carbonaceous fuel to Nutzgasen,

wherein the reaction chamber (4) comprises a plurality of at least partially independent control inputs (10) such that the gasification is controlled by the addition of gasification agents via the control inputs (10) characterized in that the added gasification agents in composition, amount, pressure, speed, temperature and / or vary with respect to their specific output pulse at individual control inputs.

marked by

a reaction chamber (4), in the interior of which a holder projects with a plurality of recessed control inputs (10).

2. Gasification reactor (1) according to claim 1,

characterized by

that during operation of the gasification reactor, each position within the reaction chamber (4) through the control inputs (10) is accessible, each control input (10) defines a reaction zone and all the reaction zones form the reaction chamber, which completely fills the reaction chamber (4).

3. gasification reactor (1) according to one of claims 1 to 2,

marked by

a reaction chamber (4) whose side walls (9) are interspersed with a plurality of control inputs (10).

4. gasification reactor (1) according to one of claims 1 to 3,

marked by

Control inputs (10), the horizontally over the reaction chamber encircling ring lines (11) to form flat, but independent, reaction zones are summarized.

5. gasification reactor (1) according to one of claims 1 to 4,

marked by

a permeable intermediate bottom (2) which divides the gasification reactor (1) into the reaction chamber (4) and into a reservoir (3) arranged above it, the reaction chamber (4) being connected via an intermediate bottom (5) to an ash box ( 6) and the ash box (6) are in turn connected to a gas outlet device (8).

Gasification reactor (1) according to one of claims 1 to 5,

marked by

a retaining device (7) between the reaction chamber (4) and the ash box (6).

Gasification reactor (1) according to one of claims 1 to 6,

characterized,

that the reservoir (3) 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 smaller than that of the reservoir (3) and the Reaction chamber (4), but greater than the opening of the intermediate bottom (5).

8. Gasification reactor (1) according to one of claims 1 to 7,

characterized, that the gasification reactor (1) and thus the reservoir (3), the reaction chamber (4) and the ash box (6) are configured overall cylindrical.

9. gasification reactor (1) according to one of claims 1 to 8,

characterized,

that the gasification reactor (1) is provided with a heat exchange device, wherein in particular the entire reactor is enclosed by a thermal insulation.