WO2007093429A2

WO2007093429A2 - Process and device for generating gas from carbonaceous material

Info

Publication number: WO2007093429A2
Application number: PCT/EP2007/001347
Authority: WO
Inventors: Jörg KEMPER; Frank Lohmann
Original assignee: Native Power Solutions Gmbh & Co. Kg
Priority date: 2006-02-17
Filing date: 2007-02-16
Publication date: 2007-08-23
Also published as: WO2007093429A3; DE102006007457B4; AR059537A1; DE102006007457A1

Abstract

For gasification of carbonaceous material (2) to form CO and H<SUB>2</SUB>-containing gas (23), first the carbonaceous material (2) is pyrolyzed and thereafter comminuted to increase efficiency, before it is gasified. For this at the outlet (33) of the pyrolysis station into the gasification reactor, a comminution unit which is preferably formed as scraper unit (71) is provided, wherein on comminution, the pyrolyzed carbonaceous material is brought to the process temperature for gasification.

Description

Method and apparatus for producing gas from carbonaceous material

The present invention relates to a method and apparatus for producing CO and H ₂ -containing gas from carbonaceous material.

Against the backdrop of decreasing resources of fossil fuels, decentralized energy supply based on waste or biomass from renewable raw materials is becoming increasingly important. In biomass or waste incineration, heat is generated, e.g. for heating buildings or water. During gasification, in addition to heat, fuel gas is generated, which can be used in engines for power generation.

The gasification generally takes place in several steps: the drying / heating in preparation, the pyrolysis and the gasification, namely the reaction of the pyrolysis products by oxidation and reduction. The resulting gas contains i.a. Hydrogen, carbon monoxide and methane, which can serve as fuel. The composition of the resulting gas depends on the reaction gas used and the temperature at which the gasification takes place. At higher temperatures, the concentration of hydrogen and carbon monoxide increases and decreases the concentration of methane.

The higher the temperature, the lower the likelihood that the resulting gas will still contain toxic or carcinogenic components such as dioxin or tar. Because at temperatures of 900 ⁰ C and higher, they are split into innocuous, volatile substances such as carbon dioxide and hydrogen. One way to high temperatures of 900 ⁰ C and to provide more, provides the use of a plasma torch.

From DE 32 33 774 A1 discloses a method and a plant for gasification of carbonaceous material to a mainly consisting of CO and H ₂ gas mixture are known in which the carbonaceous material is input in particulate form in a shaft furnace to a predetermined level. The shaft furnace has plasma torches on the ground. In addition to heat energy through the plasma torch and oxidant in the form of O ₂ , CO ₂ or H ₂ O is supplied. As a result, the carbonaceous material is subjected to a high temperature under oxidizing conditions. The volatiles are then released and react with the oxidizer. The non-volatile part is, however, coked. Oxidizer that has not reacted with the volatiles may react further down in the shaft furnace with the coke produced and additionally form CO and possibly H ₂ O. Upwardly escaping CO ₂ and H ₂ O can react with the carbonaceous material falling down to CO and H ₂ . The gas leaving the shaft furnace has a maximum temperature of 1500 ^° C. The temperature on the surface of the granular material in the shaft furnace can reach approximately 2000 ^° C.

An object of the present invention is to provide a method and an apparatus in which the carbonaceous material is treated for gasification.

This object is achieved by a method for gasifying carbonaceous material to CO and H ₂ containing gas comprising the steps of: at least partially pyrolizing the carbonaceous material; Gasification of the pyrolysis products and / or of the carbonaceous material, wherein the pyrolysis products and / or the carbonaceous material are comminuted after the pyrolysis and simultaneously brought to the process temperature for the gasification.

Crushing increases the surface area of the material to be gasified, resulting in a significant acceleration of the gasification process, such as bringing to gasification process temperature during crushing. In addition, the overall energy balance is improved. Because unlike the crushing of the starting material before the pyrolysis, for which quite a lot of energy is required, the solid pyrolysis products, which are mostly coal, with relatively little effort and reduce energy. More preferably, the pyrolyzed carbonaceous material is comminuted immediately after pyrolysis and brought to process temperature for gasification before it is appreciably cooled to further improve the overall energy balance.

Depending on the process parameters, in particular temperature and reactants, the gasification can take place auto- or allothermic. To ensure the most complete possible gasification, the gasification is preferably carried out with the aid of external heat input. It is particularly preferred to provide the external heat input by a plasma, for example an inert gas plasma or oxygen plasma. Because with the help of a plasma can easily reach temperatures, which is guaranteed that even residues of tar or harmful compounds split and in in particular CO and H _{2 are} converted. The use of steam plasma has proved to be particularly advantageous: It consists of O, H, OH, O ₂ , H ₂ and H ₂ O radicals which are very good with the pyrolysis products and possibly not yet pyrolyzed carbonaceous material. In addition, the enthalpy density of water vapor plasma is very high. These properties lead to an acceleration of the

Gasification process. In addition, since the thermal efficiency of steam plasma sources is 70-90%, the use of steam plasma is economical in operation. Advantageous is the use of both pure water vapor plasma and plasma from water vapor with additives or from gas mixtures with water vapor as a reaction accelerator.

In a preferred embodiment, the pyrolysis is carried out by means of microwave irradiation and heating. By coupling energy via microwaves into the carbonaceous material, it is achieved that the carbonaceous material is completely penetrated with little effort and heated rapidly from the inside to the outside. Moisture-containing carbonaceous material also achieves sufficient drying and conversion of the moisture to water vapor, which is then available as an oxidizing agent during gasification. Since the carbonaceous material is heated from the inside to the outside, combustion is suppressed, and instead the carbonaceous material is pyrolytically split into volatile carbon compounds and non-volatile carbon compounds with shorter carbon chains. Conventional heating means may be used to preheat the carbonaceous material from outside to inside or reheat it after or parallel to microwave irradiation. The heat input from the inside to the outside and from the outside to the inside reduces the time required for as complete pyrolysis as possible and overall improves the energy balance of the entire process. The pyrolysis products serve below as starting materials for the gasification, which is faster and more efficient due to the already at least partially carried out pyrolysis.

An important advantage is that it can be used particularly well in small-scale systems for decentralized energy supply. Because of the pretreatment by means of microwaves, for example, even household waste or biomass in the form of garden waste can be used without expensive prior treatment. Namely, the drying and heating as well as the pyrolysis are achieved largely or completely by the microwave irradiation. Also, a heating unit to support pyrolysis can be provided with only a small footprint. It has proven to be advantageous to densify the carbonaceous material before and / or during and / or after microwave irradiation. The compaction leads to a more efficient energy input by microwave irradiation and / or thermal radiation and is preferably carried out before the microwave irradiation and / or optionally before the heat radiation. As a result, as complete as possible pyrolysis of the carbonaceous material is achieved by the microwave irradiation.

In a further aspect of the present invention, the object is achieved by a device for gasifying carbonaceous material to CO and H ₂ -containing gas with a pyrolysis station and a gasification reactor in which a comminution unit is arranged in the gasification reactor, which comminutes the nonvolatile pyrolysis products. If carbonaceous material should not be completely pyrolyzed, this too is crushed by means of the comminution unit.

The arrangement of the comminution unit in the gasification reactor has the significant advantage that the material to be gasified is heated on the one hand by contact with the comminution unit, since the comminution unit has by its arrangement within the gasification reactor substantially the same temperature as the ambient temperature inside the gasification reactor, for Others can be exposed to the material to be gasified at the moment of its comminution of the ambient temperature inside the gasification reactor and because of its enlarged by the crushing surface immediately assumes the ambient temperature.

Preferably, the gasification reactor has at least one heat source with the aid of which the gasification of the comminuted pyrolysis products and of the comminuted carbonaceous material, if it has not been completely pyrolyzed, takes place. However, if suitable reducing and oxidizing agents and appropriate process conditions are selected, the gasification can also take place autothermally, so that the heat source can also be dispensed with.

In a preferred embodiment, the pyrolysis station is designed as a microwave station with heating unit in order to split the carbonaceous material into pyrolysis products as efficiently as possible and if necessary to dry and / or to heat them. Advantageously, the pyrolysis station has a compression unit. Depending on the embodiment, the compression unit may be connected upstream of or integrated in the pyrolysis station. The integration into the pyrolysis station is particularly suitable when irradiated simultaneously with microwaves and heated by radiant heat as well as to be compacted. The compaction unit allows a more compact design of the pyrolysis station, which can be thermally insulated with less effort.

In a preferred embodiment, the shredding unit is designed as a scraping unit that scrapes off the surface of the pyrolysis products and / or the carbonaceous material that is emerging from the microwave station. During the scraping operation, the scraping unit releases the gasification process temperature to the fresh scraping point of the scraped off material by direct contact. In this way the energy input into the material particles is accelerated. In addition, the scraper creates a cracked surface, which further enlarges the gasification surface.

Advantageously, the scraping unit is designed as an arrangement of blades which can be guided past the pyrolysis products and / or the carbonaceous material.

In a preferred embodiment, the scraping unit is designed as a rotatable scraping part which has perforations on the side facing the exiting pyrolysis products and / or the carbonaceous material. The edges of the apertures scrape particles from the non-volatile materials which pass through the apertures into the reactor.

For a particularly efficient scraping, the exit from the pyrolysis station is designed as a tube and projects the rotating scraping part into the tube. In order to prevent possible clogging, the scraper is arranged axially displaceable in the pipe direction.

Preferably, the scraping part of ceramic, to ensure a long life even at high gasification temperatures.

Preferably, the at least one heat source is at least one plasma torch, more preferably at least one steam plasma torch. With the help of plasma torches can reach sufficiently high temperatures that also toxic and undesirable compounds in CO and H2 are split. When using in particular water vapor plasma torches, the plasma also provides necessary oxidizing agent.

In a preferred embodiment, the plasma torch is on

Shredder directed to bring the shredder and crushed by them material to a high temperature so that the gasification can begin even during the crushing.

The present invention will be explained in more detail with reference to a preferred embodiment. Show this

Figure 1 is a perspective view of a first embodiment of a device for gas generation;

Figure 2 is a horizontal section through the device of Figure 1;

Figure 3 is a vertical section in the longitudinal direction through the device of Figure 1 in a simplified view;

Figure 4 is a vertical section perpendicular to the longitudinal direction through the device of Figure 1 in a simplified view;

Figure 5 is a schematic detail view of a first embodiment of a scraping unit;

Figures 6a, b is a schematic detail view of a second embodiment of a scraping unit from the side and in plan view;

Figure 7 is a horizontal section through a device as in Figures 1 to 4 with the scraping unit of Figures 6a, b;

Figures 8a, b is a schematic representation of a particular embodiment of the scraping unit of Figures 6a, b;

FIG. 9 schematically shows the material flow of a gasification: Figure 10 is a perspective view of a second embodiment of a

Apparatus for generating gas;

11 shows a horizontal section through a device as in FIG. 10 with the scraping unit from FIGS. 6a, b;

Figure 12 is a vertical section perpendicular to the longitudinal direction through the

Device of Figure 10 in a simplified view; and

FIG. 13 shows a vertical section through the device from FIG. 10 at the level of the pyrolysis furnace for the pyrolysis.

1 shows a gas generator 1 on a support 108, which is designed for a power of about 100 kW _e i (net). The starting material may be industrial or household waste or biomass based on renewable raw materials, such as garden waste, wood chips, preferably a grain size of about 6-20 mm, sawdust, pellets, peel, husks or straw. Even fossil fuels can be gasified in the gas generator.

The carbonaceous material is filled through the hopper 100. Using the waste heat of a gas cooler 10 in the form of a heat exchanger, possibly combined with a gas scrubber, the carbonaceous material 2 can already be preheated there to about 60 ° -80 ° C (see also reference 201, Figure 9).

With the aid of a screw conveyor 102 (see also FIGS. 2, 3) with drive 104, the carbonaceous material 2 is conveyed further into a reactor 6. There, the carbonaceous material 2 is heated to about 400-500 ⁰ C. This is done predominantly by microwaves generated in the microwave generator 31 and a heater 62 which utilizes the waste heat of the primary reactor 4 in which the gasification is taking place, or externally energized, eg as an electric furnace, or a combination of internal and external energy. The heater 62 is connected to the reactor 6 and connected upstream of the microwave generator 31.

In addition, the carbonaceous material 2 is passed through a crimping part 61 surrounded by the heater 62. The Quetschteil is conical, with being Cross section tapered in the conveying direction. As a result, the carbonaceous material 2 is compressed airtight before the microwave zone 32.

By the heater 62, the carbonaceous material 2 is heated from the outside inwards. Due to the microwave radiation in the microwave station 3, the carbonaceous material 2 is penetrated and heated from the inside to the outside. This combination of supplied radiant heat and microwave irradiation leads to the best possible heat input into the carbonaceous material 2.

Due to the heat input, the carbonaceous material 2 is also dried. This is particularly advantageous in non-pretreated starting materials such as industrial or domestic waste or garden waste, but also generally in biomass from renewable resources. The gas generator 1 is therefore insensitive to even greater fluctuations in the moisture content of the carbonaceous material 2. The moisture exits as water vapor from the carbonaceous material 2 and serves as an oxidizing agent in the gasification process.

The high heat input, in particular into the interior of the carbonaceous material 2 by the microwave irradiation, triggers the pyrolysis of the carbonaceous material 2. In pyrolysis, i.a. the longer-chain molecules of the carbonaceous material 2 are split into shorter molecules. Volatile and non-volatile pyrolysis products form, which are used as starting materials for the subsequent gasification. In order to implement the energy input by microwave irradiation more targeted, the carbonaceous material 2 is passed through a feed tube 33, so that the entire carbonaceous material 2 is guided through the microwave zone 32. Especially if pellets or similar

Biomaterial be used as starting material 2, the molecular structures are virtually broken by the microwave irradiation, whereby the pyrolysis proceeds more efficiently. The airtight compression in the pinch part 61 in front of the microwave zone 32 ensures that as far as possible no nitrogen from the ambient air enters, which would reduce the calorific value of the generated CO and H ₂ containing gas.

The dimensioning of the microwave generator 31 depends in particular on the extent of the microwave zone 32, the density of the carbonaceous material 2 and the desired temperature. The choice of frequency may be limited by government regulations. For example, in Germany only the frequencies 24.25GHz, 5.8GHz, 2.45GHz and exceptionally 915MHz are allowed for microwave heating. Instead of a microwave generator can also be used two, three or more, which can form either a coherent microwave zone or multiple separate microwave zones.

The feed tube 33 leads into the gasification reactor 4, into which also a plasma burner 5 opens and in which the gasification takes place. The feed tube 33 passes through a sieve drum 42 arranged in the gasification reactor 4. The sieve drum 42 is rotatably mounted about its longitudinal axis and is rotated via the drive 106. In the present example, the longitudinal axis of the screen drum 42 is parallel to the feed tube 33. Screen drum pockets 43 are arranged on the circumferential wall of the screen drum 42 (see in particular FIG. 4). In addition, on the side facing the plasma torch 5 side of the screen drum 42, a scraper unit 7, here in the form of five blades 71, which are carried along with the screen drum 42, while passing the exit of the feed tube 33 and the surface of the exiting material, i. the nonvolatile pyrolysis products 21 and possibly not yet fully reacted pyrolytically

Starting material 2, scrape, whereby small particles 25 are formed (see also Figure 5). In particular, the already completely pyrolyzed material is very brittle, so it can easily crumble. In addition to surface enlargement by particle formation itself, the scraping process results in a cracked and thus particularly large surface area available for the gasification process, allowing the gasification process to proceed much more quickly and efficiently.

Opposite the outlet of the feed tube 33, the hot gas stream 23 of the plasma burner 5 opens into the gasification reactor 4. Therefore, the scraped off particles 25 are exposed directly to the hot gas stream 23. In addition, the blades 71 of the scraping unit 7 constantly pass through the hot gas stream 23, so that they also have the process temperature of about 950 ° -1050 ° C and leave the direct contact with scraping this temperature to the supplied pyrolysis products 21 and possibly the carbonaceous material 2 , As a result, the particles 25 in the shortest possible time to process temperature and can be gasified. The temperature of 950 ^cC and more in the gasification zone ensures that even harmful carbon compounds and tar are completely gasified and also the content of CO and H _{2 in} the gasification product is as high as possible.

Turbulences prevail in the hot gas stream, leading to a rapid mixing of the scraped off particles with the remaining reactor contents, ie with the reactants for lead the gasification. As a result, the gasification takes place faster and more intensively, whereby the overall efficiency is increased. Particles 25, which sink in the reactor interior and remove from the hot gas stream 23, are collected by the screen drum 42 in their compartments 43, transported back to the hot gas stream and poured there in the hot gas stream, so that they are better available again for gasification. The entire reactor contents are constantly circulated, which further promotes gasification.

A further embodiment of a scraping unit is shown in detail in FIGS. 6a, b and as part of the gas generator in FIG. It is a rotating scraper 72, which is arranged at the outlet of the feed tube 33. The scraping part 72 consists of a ceramic disk with windows 75 arranged on the front side. In contrast to the scraping unit 7 with blades 71 which is driven via the screening drum 42, the rotating scraping part 72 is driven via a shaft 73. Due to the rotational movement of the non-volatile pyrolysis 21 particles 25 are scraped off. These fly through the frontal windows 75 from the feed tube 75 into the hot gas stream 23 of the

Plasma torch 5. Since the volatile pyrolysis products as well as the water vapor already formed during drying also have to escape through the windows 75 from the feed tube 33, intensive gasification already takes place in the region of the windows 75, which act like small reactor chambers. As a result, the overall efficiency of the gas generator 1 is further increased.

A particular embodiment of a rotating scraping part is shown in FIGS. 8a, b. The rotating scraping part 72 'has radially arranged windows 74 in addition to the windows arranged on the front side. It rotates in the feed tube 33 and is driven as above via the shaft 73.

The drive 105 of the rotating scraping member 72 'consists essentially of a drive bushing 81, which is rotatably mounted in a housing (not shown). The rotational movement takes place in the present example, a sprocket 87. Likewise, but also a gear, a toothed belt, a V-belt or the like can be used. The shaft 73 is guided radially in the drive bush 81, but can move axially. At the right end of the shaft 73 is positively and / or positively secured a driving star 82 and secured by screw 86. The driving star 82 engages in circularly arranged grooves in the drive bushing 81. As a result, the rotational movement of the drive bush 81 transmits to the shaft 73. Axially, the driving star 82 can move within the grooves. The axial movement is to the right by a rear Travel limit 83, which is bolted to the drive sleeve 81, limited. To the left, the axial movement against the force of a spring 84 to the end of the grooves in the drive bushing 81 is possible.

FIG. 8a shows the normal operation of the rotating scraping part 72 '. As it rotates, the follower 82 is located at the rear travel limit 83 and the radial windows 74 are covered by the walls of the delivery tube 33. In FIG. 8b, the axial pressure on the rotating scraping member 72 'increases due to impending clogging of the delivery pipe 33. If the axial force of the rotating scraping member 72' exceeds the force of the spring 84, the rotating scraping member 72 'moves leftward out of the drawing

Feed tube 33 and thus releases the radially arranged windows 74. Nonvolatile pyrolysis products 21 can now escape from the feed tube 33 through the windows 74 and prevent their clogging.

By a sensor 85 in the region of the drive bush 81, the axial position of the driving star 82 can be defined and thus counteracted via a control of the input variables "speed of the scraper" and "speed of material supply" the risk of clogging. In addition, the displacement measurement of the driving star 82 allows a determination of the state of wear of the rotating blade part 72.

Plasma torch 5 in the present example is a steam plasma torch. The composition of the steam plasma promotes the gasification process very strongly, which consists of the radicals O, H, OH, O ₂ , H ₂ and H ₂ O at a mean temperature in the range of 4000 ⁰ C and peak values in the core of the plasma flame of approx. 12000 ⁰ C. The enthalpy density of water vapor is very high and the thermal efficiency of water vapor sources is 70% -90%. In addition, water vapor is readily available. Water vapor plasma therefore not only has an accelerating effect on the gasification process, but is also advantageous for economic reasons.

In order to shorten the residence time of the particles 25 until the gasification is as complete as possible, reactor contents of the plasma flame 51 are supplied via line 41 (FIG. 3). There, the gasification takes place particularly intense. In addition, this leads to a circulation of the reactor contents, since the plasma flame 51 supplied mixture of gas and particles 25 enters as hot gas stream 23 back into the reactor interior and there leads to turbulence and improved heat transfer to the newly supplied particles 25. In the reactor 4, the mixture of gas and particles also hits the scraping device 7 and the surface of the supplied pyrolysis products 21, possibly also of the carbonaceous material 2, and heats them to the process temperature. Subsequently, it flows into the lateral upper region of the screening drum 42 and mixes with the material constantly conveyed up through the screening drum. This will maintain a continuous gasification process. This gasification process also speeds up the gasification process.

All of these measures lead to a very greatly reduced residence time of the material to be gasified. As a result, in particular the gasification reactor 4 can be dimensioned significantly smaller, with the result that the insulation losses are greatly reduced and the overall efficiency can be significantly increased. The size of the gas generator can be so greatly reduced that in addition to systems in the power range of about 100 kW _e i (net) and more small systems for residential use in the power range of about 2-4 kW _e ι (net) are possible.

The ash 24 produced during the gasification is screened off through the sieve drum 42 and falls into the lowermost region of the gasification reactor 4. There is an ash outlet 1 14, through which the ash 24 is discharged (reference numeral 203 in Figure 9). The remaining gasification products 23 are withdrawn via the lower reactor region by means of a slight negative pressure by means of a blower 128 from the reactor interior to a filter unit 112. Advantageously, these are ceramic filter candles 1 13, which may be integrated into the reactor housing. The ceramic filter cartridges 113 serve as dust filters and have the advantage that the gas generated can be filtered without prior cooling, ie at about 700 ° -800 ° C.

After filtering, the generated hot gas for power generation could be fed directly to a hot gas engine or even to a pore burner. In the present example, the hot gas is passed via a line 122 to another station 120, which has the function of a gas-water heat exchanger and / or a scrubber. This allows the hot gas to cool to below 50 ⁰ C and clean. In addition, the heat can be used by the warmed up cooling water, which is fed via the input 1 16 and the output 118 is derived, is fed by means of a pump 126 in the building technology or forwarded to an external heat exchanger. The heat can also be used for preheating the carbonaceous material. 2 use. The cooled clean gas is withdrawn by means of the blower 128 via a negative pressure from the system and removed for further use in an external gas storage or a combined heat and power plant.

The second apparatus for producing gas shown in FIG. 10 differs from the first apparatus shown in FIG. 1, in particular with regard to the design of the pyrolysis station. While in the first device, the material to be pyrolyzed after compaction is first heated with the aid of the heater from outside to inside, before it is irradiated with microwaves to heat it from the inside out (see also Figures 2 and 3), is in the second device, the material to be pyrolyzed first irradiated with microwaves of the microwave generator 31 to reach the inside of the pyrolysis, and then by a heater, in this example, a porous furnace 63, out to bring the material also from the outside to the pyrolysis temperature ,

FIG. 13 shows a vertical section through the device from FIG. 10 at the level of the porous burner 63. In this example, for more intensive pyrolysis, the microwave station is combined with three porous burners 63 which adjoin the microwave generator 31 and around the feed tube 33 are arranged in the region of the lower circumference, so that the radiant heat 66 radiates onto the feed tube 33. The pore burner 63 may be fired with syngas generated in the gas generator and containing CO ₂ and H ₂ , which is supplied via the synthesis gas ports 64. The synthesis gas is burned together with air or oxygen in the pore area of the pore burners 63 to generate thermal energy. The resulting exhaust gases exit through the discharge outlet 65 and can be used for preheating other components. The pore area is generally formed of ceramic foam or other high temperature resistant structure. Particularly advantageous for pore burners is their very high power density of about 1000 kW / m ² . In particular, high temperatures of up to about 1400 ° C can be achieved. Further advantages are high heating rates and good controllability of the oven temperature. Since pore burners allow very high gas temperatures, gas generated during the gasification process can be supplied to them immediately without prior cooling, if necessary after dust filtration. In the example shown in FIG. 13, the porous burner 63 achieves a heat input that is six times higher than that of a conventional gas burner. Overall, the use of a pore burner in combination with microwave pyrolysis improves the overall energy balance of the pore burner Gas burner with still small footprint and is therefore particularly suitable for gas generators, which are sized for home use.

Furthermore, in the gasification reactor 4 of the second device (see FIG. 11) there are some differences from the first device: The feed tube 33 for feeding the pyrolyzed material and the plasma torch 5 are arranged relative to one another such that the hot gas flow generated by the plasma flame 51 is not only laterally but frontally on the scraper unit 72 (see also Figures 6a, b) meets to heat the scraper unit 72 even better. During scrape, the scraper unit 72 transfers its temperature to the material to be shredded. Due to the frontal orientation of the hot gas stream 23 on the scraper unit 72, it is also better achieved that the hot gas stream in the front windows 75 of the scraper unit 72 also directly heats the material to be shredded to the process temperature for the gasification.

The heating of the pyrolysis immediately after pyrolysis, even if they are due to the pore burner at a very high temperature, leads to the fact that already takes place in the feed tube 33 to the gasification reactor side exit gasification already. Also in the frontal windows 75 of the Schabeineinheit 72 already partial gasification takes place.

The advantage of this smooth transition from pyrolysis to gasification is that the solid pyrolysis products are gasified very efficiently and little ash remains. Therefore, even in the second device shown here, the drum 45 is not designed as a sieve drum, but only as a drum 45 with drum compartments 43 (see Figure 12) to bring not yet gasified particles 25 back into the hot gas stream. The few ash 24 can exit via the end faces of the drum 45 and be discharged via the ash outlet 114. The non-perforated drum 45 has the additional advantage of more efficient thermal insulation of the interior of the gasification reactor 4.

The plasma flame 51 is arranged in the second device in a diffuser 52 provided with openings 53 (see FIG. 11). In the water vapor plasma flame 51, the volatile and solid pyrolysis products come together with the radicals generated there, with which they react to CO and H ₂ . In addition, they are heated very rapidly in the plasma very rapidly, so that a sudden volume expansion takes place, which leads to a local negative pressure. Through the openings 53 are on this local vacuum another Pyrolysis products are sucked into the water vapor plasma flame 51, so that a constant flow of hot gas is maintained.

By shortening the feed tube 33 and the intrusion of the plasma torch 5 into the gasification reactor 4 compared to the first device, the space requirement is further reduced in the second device.

It should be noted that the second apparatus for producing gas from FIGS. 10 to 13 can also be executed with the scraping unit 72 'as in FIGS. 8a, b or also with blade 71 as in FIG. 4 or another scraping unit.

It should also be noted that also in the second gas generating device, the generated hot gas can be further used as described above.

REFERENCE CHARACTERS

1 gas generator

10 house plant

2 carbonaceous material

21 non-volatile pyrolysis products

22 volatile pyrolysis products

23 hot gas flow

24 ash

25 scraped off particles

3 microwave station

31 microwave generator

32 microwave zone

33 feed tube

4 gasification reactor

41 recirculating air duct

42 sieve drum

43 screen drum compartment

45 drum

5 plasma torches

51 plasma flame

52 diffuser

53 opening

6 reactor

61 pinch piece

62 heating

63 pore burners

64 gas connection

65 exhaust gas outlet

66 radiant heat

7 scraping unit

71 blade

72, 72 'rotating scraper

74 radially arranged window

75 frontally arranged window

81 Drive book

82 driving star 83 rear limit

84 spring

85 sensor

86 Screw connection 87 Sprocket

100 funnels

102 transport screw

104 Drive screw conveyor

105 Drive Rotating scraper 106 Drive sieve drum

108 edition

110 heat exchanger / scrubber

112 filter unit

113 ceramic filter cartridge 114 ash outlet

116 cooling water inlet

118 cooling water outlet

120 clean gas outlet

122 Gas line 124 Infeed in building technology / external heat exchanger

126 pump

128 blowers

130 external gas storage / combined heat and power plant / engine

Preheat 201 203 Ash discharge

Claims

claims

A method of gasifying carbonaceous material to CO and H ₂ containing gas comprising the steps of: at least partially pyrolizing the carbonaceous material;

Gasification of the pyrolysis products and / or of the carbonaceous material, characterized in that the pyrolysis products and / or the carbonaceous material are comminuted after the pyrolysis and simultaneously brought to the process temperature for the gasification.

2. The method according to claim 1, characterized in that the gasification is carried out by means of external heat input.

3. The method according to claim 2, characterized in that the external heat input is performed by a plasma, in particular a water vapor plasma.

4. The method according to any one of claims 1 to 3, characterized in that the pyrolysis is carried out by means of microwave irradiation and heating.

5. The method according to any one of claims 1 to 4, characterized in that the carbonaceous material is compacted before and / or during and / or after the microwave irradiation.

6. A device for gasifying carbonaceous material to CO and H ₂ -containing gas with a pyrolysis station and a gasification reactor, characterized in that in the gasification reactor (4) a crushing unit (7, 71, 72, 72 ') is arranged, which the non-volatile pyrolysis (21) crushed.

7. Apparatus according to claim 6, characterized in that the gasification reactor (4) has at least one heat source (5).

8. Apparatus according to claim 6 or 7, characterized in that the pyrolysis station is designed as a microwave station (3) with heating unit (62).

9. Device according to one of claims 6 to 8, characterized in that the pyrolysis station (3) has a compression unit (61).

10. Device according to one of claims 6 to 9, characterized in that the comminution unit as a scraping unit (7, 71, 72, 72 ') is formed, which is the surface of the pyrolysis products (21) emerging from the pyrolysis station (3), scrapes.

11. The device according to claim 10, characterized in that the scraping unit as an arrangement of the pyrolysis products (21) passable blades (71) is formed.

12. The device according to claim 1 1, characterized in that the scraping unit as a rotatable scraper part (72, 72 ') is formed, which on the the exiting

Pyrolysis products (21) facing side openings (74, 75).

13. The apparatus according to claim 12, characterized in that the outlet from the pyrolysis station (3) is designed as a tube (33) and the rotating scraper part (72, 72 ') protrudes into the tube (33).

14. The apparatus according to claim 13, characterized in that the scraping part (72, 72 ') is arranged axially displaceably in the tube direction.

15. Device according to one of claims 12 to 14, characterized in that the scraping part (72, 72 ') is made of ceramic.

16. Device according to one of claims 6 to 15, characterized in that it is the at least one heat source to at least one plasma torch (5).

17. The apparatus according to claim 16, characterized in that it is at least one water vapor plasma torch (5).

18. The apparatus of claim 16 or 17, characterized in that the plasma torch (5) on the comminution device (7, 71, 72, 72 ') is directed.