EP0609802A1 - Continuous devolatilisation and/or gasification of solid fuels or wastes - Google Patents

Abstract

In a process and equipment for the continuous gasification/devolatilisation of a lumpy, sorted and dressed fuel/waste material in a shaft-type reactor (3), the charge, gaseous gasifying agent and produced gaseous fuel are passed downwards in cocurrent and the gasifying agent (6) is preheated in a helical countercurrent heat exchanger (21; 22), located in the jacket part, by the gaseous fuel (7) and further heated in helical or corrugated channels (25; 23; 35) in the ceramic hearth body (8) and in a movable or fixed, conical or paraboloid central body (10) which serves as hearth closure and protrudes into the lower part of the charge. The grate is formed by a solid cone (10) or by a rotatable, vertically displaceable counterpiece which represents a hollow-conical annular body (47; 50) and which leaves open an adjustable annular passage (15) opposite the lower hearth part for the escape of the generated gaseous fuel (14; 26) and for discharging (16) the solid or liquid reaction products in the form of ash, slag and/or distillation residues. <IMAGE>

Description

Technical field

Degassing and gasification of solid organic energy sources for the purpose of conversion into gaseous energy sources.

The invention relates to the degassing and gasification of solid carbon-containing fuels and waste materials and an apparatus suitable for this, which meets the various ecological and operating conditions, for the continuous provision of a gaseous secondary fuel.

In the narrower sense, the invention relates to a process for the continuous, at least partial conversion of a solid, lumpy fuel or combustible waste material into a gaseous fuel by presorting, processing, at least partially degassing and / or at least partially gasifying in a vertical-axis shaft-like reactor, the starting material being in the form a feed column that slides down, successively a preheating and drying zone, a degassing zone, an oxidation zone and a reduction zone passes through, the preheated gaseous gasification agent is injected centrally into the lower part of the interior of the feed column and the gaseous and vaporous reaction products produced by degassing and gasification, which finally form the desired gaseous fuel, are passed downwards in a direct current to the feed column, diverted upwards and redirected and on the outside of the reactor wall, in a vertical direction, countercurrently to the feed column.

The invention further relates to a device for carrying out the method of at least partial degassing and / or at least partial gasification of a pre-sorted, prepared solid particulate fuel or combustible waste material, the device comprising a vertical-axis shaft-like reactor with a gas-tight charging device and gas-tight ash discharge or slag discharge device , further consists of an introduction of the gaseous gasification agent and a discharge of the gaseous fuel to be produced, as well as of heat exchangers, in such a way that an at least partially provided with a highly refractory lining reactor shaft and a downwardly narrowing narrowing refractory ceramic stove, the underside of which with a Grate with a variable passage cross-section, vertically displaceable, rotatable ceramic counterpart is lockable, furthermore a triple cylindrical jacket s and how a freely movable reactor shaft suspension is provided.

State of the art

Methods and devices for continuous or intermittent degassing and gasification of solid fossil fuels are in the form of gas generators, Wood gasifiers and other devices and the processes carried out with them are known in very large numbers. A distinction is made between processes and equipment for continuous or intermittent operation, for lumpy or fine-particle use and for processing coal or wood. For the gasification of coal with a small proportion of volatile and condensable components, the ascending gasification in countercurrent to the charging column is mostly used, while for the gasification of wood and peat, which provide a high proportion of condensable components (tars, alcohols, acetic acid etc.) descending gasification in direct current to the feed column is preferred. In the latter, the vapors of the condensable constituents which are undesirable for the production of a pure generator gas as secondary fuel are passed through the hot ember bed in the lower part of the feed column, thermally decomposed, pyrolytically split and reacted with the carbon to form harmless low-molecular gases. These chemical reactions require a certain minimum temperature for thermodynamic and reaction kinetic reasons. This relates both to the average maximum temperature achieved in the charging column and to the local absolute maximum temperature. There has been no shortage of decades of attempts to implement the so-called high-temperature gasification. For this purpose, the gasification agent (usually air) must be fed to the charging column in a centrally concentrated manner. The usual designs of gas generators with peripheral nozzles in the stove for the supply of the gasification agent are less suitable for this. However, the attempted central feeding mostly failed due to the material problem. Metallic materials (without active cooling) are no longer suitable for the local maximum temperatures of over 1500 ^o C that occur. Conventional ceramic materials mostly dropped out because of their brittleness.

Another topic is the perfect operational control of the discharge of solid and / or liquid products at the lower end of the range. The so-called grate serves as the closing organ - based on the firing system - which causes the ashes to fall through or the slag to run off or, if necessary, to remove the high-carbon components (coke, charcoal) that are not to be gasified. Numerous grate constructions, including rotary grates, have become known, which were mostly made of metallic materials and could not be fully satisfied due to limited heat resistance and insufficient high-temperature corrosion resistance. In recent times, the problem has been solved in a good approximation by a rotatable, conical ceramic body. The throughput of the primary fuel can be regulated within wide limits by means of the annular gap formed by this body together with the stove and intended for the discharge.

Executed gas generators for wood as an insert usually work in direct current with descending gasification and use the jacket for the limited preheating of the air usually used as a gasifying agent. Additional air preheating devices in the area of the range have also been proposed, or attempts have been made to keep the latter below tolerable temperatures by means of special cooling air. Central air supply pipes for introducing the gasification agent into the inside of the charging column from above, from the side or from below have already been implemented. However, their probation usually failed due to an inadmissible hindrance to the downward movement of the feed and led to blockages, channel formation or the notorious "hanging" of the latter. An effective one Air preheating in the central air supply pipe has been attempted only in exceptional cases and generally only related to a partial air flow. Their effect is also very doubtful. In numerous proposed devices, air preheating was dispensed with at all, so that neither a high gasification temperature nor a high degree of efficiency can be expected. For the partial cooling of the gases generated, the jacket of the reactor shaft is usually used at least partially by passing the gas through a hollow cylindrical annular space. This type of gas cooling is very incomplete due to the low gas velocities, so that further heat losses must be expected here. The grate is located inside or below the hob area of the gas generator, which often caused malfunctions and difficulties. In addition to the usual fixed, lattice or fence-like grate constructions, movable designs in the form of plate-like rotating grates, chain-like traveling grids or openwork single or multiple rollers have become known. Despite the partly very extensive mechanization of such devices, they never quite satisfied. A reasonably safe ash discharge can be guaranteed with this, but its repercussions on the stacking column above it and thus its favorable influence is minimal.

It has been attempted for a very long time to partially or completely degas primary fuels in a continuous manner in order to produce more suitable solid secondary fuels such as coke, semi-coke, charcoal, etc. Most of the devices proposed for this had a shaft-like structure and were made entirely of refractory bricks. In one case, they were heated from the outside, which is relatively thin, mechanically sensitive ceramic walls and a lot of effort in terms of heating energy. In the other case, the charging column was heated from the inside by partial combustion of the primary fuel, which resulted in a comparatively poorer gas and left something to be desired in terms of optimal control of the degassing process, particularly with regard to temperature distribution. The discharge organs were often poorly designed and hardly allowed the behavior of the loading column to be influenced in the sense of achieving optimal mechanical and thermodynamic conditions. The above-mentioned methods and devices were therefore unable to replace the traditional chamber furnaces of the gas works and coking plants and the traditional coal kiln.

The foregoing clearly shows that despite decades of practice in the field of converting carbon-containing solid primary energy sources into more suitable gaseous or partially gaseous, partially solid secondary fuels, a suitable, universally applicable process and the corresponding versatile and adaptable device for its economical implementation are largely lacking.

The disposal and further treatment of waste of all kinds, in particular garbage, rubbish, etc. has recently become a serious problem for both ecology and economics. Sooner or later the landfill sites that are usual will no longer be permitted due to their harmful impact on the environment. Therefore, with regard to the disposal of combustible waste materials, more and more have been switched to so-called waste incineration plants. Due to its partially toxic emissions, this process is now also at risk of getting into trouble. In addition to the poor utilization of the thermal energy generated, such systems must increasingly use expensive catalyst batteries and other gas cleaning and gas conversion devices. The changeover to processes other than incineration is therefore currently an imperative.

• US-PS 4 344 772
• US-PS 4 306 506
• US-PS 4 309 195
• US-PS 4 389 222
• CH-PS 678 973

Die bisher üblichen und bekannten Entgasungs- und Vergasungsverfahren und die entsprechenden, zu ihrer Durchführung marktgängigen Geräte lassen in vieler Hinsicht zu wünschen übrig. Ein weiterer Aspekt ist die zurzeit unbefriedigende Situation auf dem Gebiet der Abfall- und Müllbeseitigung und -Verwertung, die dringend nach besseren ökologischen Lösungen verlangt. Es besteht daher ein grosses Bedürfnis zur Weiterentwicklung, Vervollkommnung und Universalisierung der genannten Verfahren und Vorrichtungen sowie deren Anwendungen.The following publications are cited regarding the prior art:

• U.S. Patent 4,344,772
• U.S. Patent 4,306,506
• U.S. Patent 4,309,195
• U.S. Patent 4,389,222
• CH-PS 678 973

The previously known and known degassing and gasification processes and the corresponding devices customary for their implementation leave much to be desired in many respects. Another aspect is the currently unsatisfactory situation in the field of waste and garbage disposal and recycling, which urgently calls for better ecological solutions. There is therefore a great need to further develop, perfect and universalize the methods and devices mentioned and their applications.

Presentation of the invention

The invention has for its object to provide a method and an apparatus for the continuous, at least partial degassing and / or gasification of a lumpy primary carbon-containing solid energy source in the form of a fuel and / or combustible waste material in a shaft-like reactor, which is as simple as possible in process control and plant can be used universally and directly, without additional cleaning, dedusting and detoxification devices and catalytic converter batteries supply a gaseous fuel which is as pure as possible and which can be used directly for motor, chemical, metallurgical or heating purposes. The method should have the highest possible efficiency and make maximum use of the exergy content of the primary energy source while avoiding the usual losses. The device is said to be particularly suitable for processing organic waste such as rubbish, garbage, sewage sludge, wood and paper waste, etc. and to enable rapid adaptation to the various input materials without loss of time or business interruption.

This object is achieved in that, in the process mentioned at the outset, the gaseous gasification agent is first guided and heated at high speed in a helical, downward movement in countercurrent to a corresponding upward helical movement of the gaseous fuel produced within the jacket section of the shaft-like reactor, also in a helical motion through the interior of a stove body with a high heat capacity and further heated, deflected vertically upwards at the lower end of the reactor and after passing through an artificially extended distance while simultaneously heating further inside a central body protruding from below into the lower part of the charging column the latter is injected, and that the gaseous fuel produced leaving the charging column is expelled downward through an annular passage is reduced and conducted at high speed in countercurrent to the gasification agent and cooled, and that the high heat capacity of the hearth body is used to bridge interruptions in operation and to carry out intermittent processes which require a certain temperature program and are superimposed on the continuous process.

The object is further achieved in that in the above-mentioned device for supplying the gaseous gasification agent between its introduction and its discharge into the charging column, a series of heat exchangers, which are arranged in succession and are arranged locally in a falling direction and which consist essentially of cylindrical or conical basic shapes, consist of increasing temperature is provided, and that a ceramic central body for guiding and injecting the gaseous gasification agent from below into the lower part of the charging column is provided, which projects comparatively deep into the latter.

Way of carrying out the invention

The invention is described with reference to the following exemplary embodiments, which are explained in more detail by means of figures.

Fig. 1

eine prinzipielle schematische Darstellung der Materialströme des Verfahrens (Fliessdiagramm),

Fig. 2

einen schematischen Längsschnitt (Vertikalschnitt) durch den prinzipiellen Aufbau der Vorrichtung mit den Strömen der gasförmigen Medien (perspektivisch),

Fig. 3

einen vereinfachten Längsschnitt (Vertikalschnitt) durch die Vorrichtung,

Fig. 4

einen schematischen Vertikalschnitt durch die Mantelpartie des Reaktorschachts mit einer ersten Ausführung des Wärmeaustauschers,

Fig. 5

einen schematischen Vertikalschnitt durch die Mantelpartie des Reaktorschachts mit einer zweiten Ausführung des Wärmeaustauschers,

Fig. 6

eine perspektivische Darstellung einer ersten Ausführung des Vollkegels als Gegenstück, Herdabschluss und Rost mit Führung des Vergasungsmittels,

Fig. 7

eine perspektivische Darstellung einer zweiten Ausführung des Vollkegels als Gegenstück, Herdabschluss und Rost mit Führung des Vergasungsmittels,

Fig. 8

einen schematischen Längsschnitt einer Rohrverbindung für Umlaufgasführung, zusätzlich mit Wärmeaustauscher,

Fig. 9

einen Längsschnitt (Vertikalschnitt) durch eine Ausgestaltung der Herd/Rostpartie mit feststehendem konischen Zentralkörper,

Fig. 10

einen Längsschnitt (Vertikalschnitt) durch eine Ausgestaltung der Herd/Rostpartie mit feststehendem parabolischen Zentralkörper.

It shows:

Fig. 1

a basic schematic representation of the material flows of the process (flow diagram),

Fig. 2

a schematic longitudinal section (vertical section) through the basic structure of the device with the streams of the gaseous media (in perspective),

Fig. 3

a simplified longitudinal section (vertical section) through the device,

Fig. 4

2 shows a schematic vertical section through the jacket section of the reactor shaft with a first embodiment of the heat exchanger,

Fig. 5

a schematic vertical section through the Shell section of the reactor shaft with a second version of the heat exchanger,

Fig. 6

1 shows a perspective view of a first embodiment of the full cone as a counterpart, stove top and grate with guidance of the gasification agent,

Fig. 7

a perspective view of a second embodiment of the full cone as a counterpart, stove top and grate with guidance of the gasification agent,

Fig. 8

2 shows a schematic longitudinal section of a pipe connection for circulating gas routing, additionally with a heat exchanger,

Fig. 9

a longitudinal section (vertical section) through an embodiment of the stove / grate section with a fixed conical central body,

Fig. 10

a longitudinal section (vertical section) through an embodiment of the stove / grate section with a fixed parabolic central body.

1 is a basic schematic representation of the material flows of the process (flow diagram). It is a specifically organized treatment and processing of essentially carbon-containing primary energy sources with the greatest possible consideration of ecological and economic conditions (environmental conditions). In principle, the process consists of separating out, reading out and separating out the resulting starting materials, branching off non-combustible materials, preparing and mixing the real primary energy sources pre-concentrated in this way in one Intermediate product, optionally comminuting or vice versa compacting for the production of a lumpy feed suitable for further processing for a thermal reactor and degassing or gasifying the latter into a gaseous secondary fuel. The latter results from optimal process control with the highest possible purity, so that it can be used directly in thermal machines (piston machines, gas turbines), used in furnaces or heaters or used as a reducing agent for chemical and metallurgical purposes. The diagram requires no further explanation.

2 shows a schematic longitudinal section (vertical section) through the basic structure of the device with the flows of the gaseous media (in perspective). The arrow indicated above and pointing vertically downward represents the task of the feed in the form of lumpy fuel. 2 is the introduction of the gaseous gasifying agent (in the present case preferably atmospheric air) into the shaft-like reactor 3 (essentially a cylindrical wall), also abbreviated as reactor shaft. The flow of the gasification agent is shown throughout as a solid solid line, that of the gaseous secondary fuel generated as a broken dash-dotted line. 4 is the outer jacket of the shaft-like reactor, 5 the discharge of the gaseous fuel to be generated. 6 represents the helical guidance (trajectory) of the gaseous gasification agent in the jacket section of the reactor. 7 is the corresponding, locally interposed helical guidance of the gaseous fuel in the jacket section, which takes place in counterflow to FIG. 6. It is a matter of heat transfer along a helical heat exchanger, the flow of the gasification agent being heated (preheating) and that of the gaseous fuel being cooled becomes. With 8 the stove or specifically the refractory ceramic stove body is called. 9 is the helical guidance of the gasification agent in the hearth body 8 for the purpose of further heating. 10 represents a full cone as a counterpart to the stove, stove top and grate, which protrudes from below into the charging column. In the present case, the full cone 10 is rotatable about its axis and vertically displaceable in its longitudinal direction. 11 is the vertically upward feed of the gasification agent into the full cone 10, 12 the helical guide and the arrow 13 the vertical discharge of the gasification agent from the full cone (injection into the interior of the feed). 14 represents the gaseous fuel that is generated in the feed and flows vertically downwards. The latter is deflected and directed vertically upwards between the cooker 8 and the outer jacket 4. Between the cooker 8 and counterpart (in the present case full cone 10) there is the annular passage 15 forming the grate, the cross section of which is adjustable. 16 is the discharge of solid and / or liquid reaction products which, depending on the management, consists of ash, slag and solid distillation residue (coke, semi-coke, charcoal, partially degassed carbon-containing product).

3 shows a simplified longitudinal section (vertical section) through the device. The reference numerals 1, 2, 3, 4, 5, 8, 10, 11, 13 and 16 correspond exactly to those in FIG. 2. At the entrance of the reactor in task 1 of the feed there is a feed device with gas-tight feed locks 51 in the form of slides lying in horizontal planes, opening or closing linearly or rotatably. The feed slides down by gravity vertically within the circular cross-section of the cylindrical wall of the shaft-like reactor 3. In the coat section of the reactor between the outer jacket 4 and the wall 3 there is a heat exchanger consisting of a helical channel 21 for the gasifying agent and a channel 22 for the gaseous fuel. In the present case, the channels 21 and 22 in helical form are nested one inside the other in the manner of a two-start thread and the gaseous media flow through them in the opposite direction. In this heat exchanger, the flow of the gasification agent is directed downwards, that of the gaseous fuel upwards. This is also indicated by the rings with dots and crosses (= arrows in cross section) of symbols 6 and 7. The full lines 6 refer to the gasification agent, the broken lines to the gaseous fuel. The lower part of the reactor shaft 3 has a refractory lining 17, while the outer jacket 4 is provided with a heat-insulating layer 28 over its entire length. The refractory hearth body 8 has a double-conical concave inner profile 18 with narrowing and is equipped along the latter with at least one conical-helical channel 25 for the gasifying agent in the form of a downward spiral. This coil serves at the same time for further preheating of the gaseous gasification agent and for cooling the hottest zone of the stove body 8. The latter is provided with a heat-insulating layer 29 on all sides on its outer boundary surface in order to reduce heat losses. After flowing through the channel 25, the gasification agent (upward feed 11) arrives via a flexible connector (not specified in any more detail) into the feed pipe 19 carrying the full cone 10 as a counterpart. The latter is firmly connected and serves as a carrier and guide for the full cone 10 Coaxial shaft 20 provided in vertical bearings. This is both rotatable and vertically slidable. The relevant drive mechanisms have been omitted for the sake of clarity. The full cone 10, which is provided on its lower end face with a heat-insulating layer 30, is provided in its interior with at least one conical-helical channel 23 (helical shape) for the gasification agent, which is located at the cone tip in the outlet opening 24 (vertical discharge 13 and injection into the feed ) ends. The gaseous fuel 14 (dash-dotted arrow) generated in the feed, flowing vertically downward, passes through the ring-shaped, rust-forming passage 15 between the cooker 8 and its counterpart (in the present case full cone 10), undergoes a deflection 26 below the cooker / grate section and arrives in the hollow cylindrical space 27 between the cooker 8 and the outer jacket 4, where it is guided vertically upwards. At the upper end of the space 27, the gaseous fuel is introduced into the helical channel 22 in the jacket section of the reactor. Via the passage 15, the solid and liquid reaction products (ash, slag, distillation residues) fall vertically downward (indicated by the vertical dashed arrow discharge 16) into the container 31 provided for this.

Fig. 4 relates to a schematic vertical section through the jacket section of the reactor shaft with a first embodiment of the heat exchanger. In the present case, there is only one layer in the radial direction. This is limited by the actual cylindrical wall 3 of the shaft-like reactor and the outer boundary 32 of the helical channels, which at the same time represents the cylindrical inside of the outer shell 4. The channels for the gaseous media, designed as helices, are nested one inside the other on the principle of a two-start thread. This takes place in the helical channel 21 for the gasification agent Flow perpendicular to the plane of the drawing towards the viewer, which is indicated by the profile of arrowhead 6 (ring with point). In the helical channel 22 for the gaseous fuel produced, the flow takes place perpendicular to the plane of the drawing away from the viewer, which is shown by the profile of the arrow end 7 (ring with cross, drawn in broken lines). The gaseous media are thus guided in opposite directions (countercurrent principle), so that optimal heat transfer is ensured and the gaseous fuel produced leaves the reactor at the lowest possible temperature. Average velocities of the gaseous media of approx. 3 m / s are aimed for. 28 is the heat-insulating layer of the outer jacket 4.

5 shows a schematic vertical section through the jacket section of the reactor shaft with a second embodiment of the heat exchanger. In this case there are two layers in the vertical direction. They are delimited by the actual cylindrical wall 3 of the shaft-like reactor, the heat-conducting intermediate jacket 33 and the outer boundary 32 of the helical channels, which simultaneously represents the cylindrical inside of the outer jacket 4. The channels for the gaseous media, which are designed as helices, are put over one another on the principle of two radially arranged threads (external thread + internal thread). In the present case, the helical channel 21 for the gasification agent is axially offset by half the slope relative to the channel 22 for the gaseous fuel, in order to make the construction more favorable in terms of strength on the one hand and freedom from tension on the other hand. With regard to flows of the gaseous media (arrow tips 6 and arrow ends 7 in profile), the statements made under FIG. 4 apply. This is also the countercurrent principle. The function of thermal insulation Insulating layer 28 goes without saying.

Fig. 6 relates to a perspective view of a first embodiment of the full cone as a counterpart, stove top and grate with guidance of the gasification agent. 10 shows the full cone, which acts as a counterpart, stove top and grate and protrudes from below into the interior of the lowest part of the charging column. The full cone 10 has cavities for guiding and further heating the gasification agent (usually air). In the present case, there is a single contiguous cavity in the form of a helical channel 23 with a circular cross-section lying on a virtual conical surface. Of course, the cross section can also have a different shape, e.g. that have a hexagon or square etc. 34 is the inlet opening on the lower end face of the full cone 10, 24 is the outlet opening for the gasifying agent located opposite the cone tip. For the sake of clarity, the representation is deliberately chosen so that the full cone 10 appears transparent, while the channel 23 acts like a spiral made of solid material. This corresponds to the hollow shape required on the one hand in the production of the ceramic body and the necessary solid core on the other hand.

Fig. 7 shows a perspective view of a second embodiment of the full cone as a counterpart, stove top and grate with guidance of the gasification agent. 10 represents the full cone, the functions of which are identical to those described in FIG. 6. The only contiguous cavity for guiding the gasification agent here has the shape of a wavy channel 35 lying on a virtual conical surface and having a circular cross section. 34 and 24 correspond to the reference numerals of FIG Fig. 6. The representation of the full cone 10 as a hollow shape and the channel 35 as a solid core also corresponds to that of Fig. 6. The same applies to what has been said about channel cross sections.

In Fig. 8 is a schematic longitudinal section of a pipe connection for circulating gas, also shown with a heat exchanger. At the edge of the left half of the figure, the contour of the shaft-like reactor is indicated in thin lines. The reference numerals 3, 10, 18 and 27 correspond exactly to those in FIG. 3. The dash-dotted arrow 36 means the circulation gas is withdrawn from the lower part of the charging column (in the present case in the lower part of the oven space). The recycle gas is used to heat the feed more effectively. Accordingly, 37 represents the recycle gas return to the top of the feed column. 38 is the corresponding pipeline for the recycle gas. 39 is the required hot gas blower, which is designed for a temperature of at least 800 ^o C. It advantageously has a rotor made of highly refractory ceramic material with high heat resistance and high temperature corrosion resistance. The pipeline 38 and the hot gas blower 39 are provided with a heat-insulating covering.

In the right part of the figure, a counterflow heat exchanger 41 for circulating gas is additionally shown as an option. It consists of two chambers separated by a heat-conducting partition 44 and is used, if necessary, for further heating of the recycle gas 42 (dash-dotted arrow). The heating gas 43 moves in countercurrent to the latter (dashed arrow). The heating gas can be a specially provided fuel gas or a high-temperature exhaust gas. The heat flow Q̇ is indicated by the arrow 45. This additional device can be used to increase the performance and efficiency of the entire system.

9 shows a longitudinal section (vertical section) through an embodiment of the hearth / grate section with a fixed conical central body. 3 is the actual shaft-like reactor (cylindrical wall, inside), 4 is the outer jacket of the reactor. The cooker 8 consists of two rotationally symmetrical, coaxially arranged ceramic parts. The outer part has a cylindrical outer surface and a double-conical inner profile 18. The inner part is cylindrical in the lower part and conical in the upper part and has a central channel for guiding the gasification agent. At the cone tip of this central body there is the vertically upward-pointing outlet opening 46 for the gasifying agent. In the space between the outer part and the inner part of the cooker 8 forming the central body there is the hollow-cone-shaped ring body 47 delimited by an outer cone and an inner cylinder as a counterpart, stove top and grate. The ring body 47 is rotatably and vertically displaceably mounted (not shown) and, together with the lower part of the outer part of the cooker 8, forms an annular passage 15 which forms the grate and through which the solid and liquid reaction products are discharged. Both the outer part and the inner part (central body) of the cooker 8 preferably have a helical channel (helix) for the gasification agent similar to FIG. 3 (25 and 23) (not shown in this figure).

10 is a longitudinal section (vertical section) through an embodiment of the hearth / grate section with a fixed parabolic central body. The shaft-like reactor 3 and its outer jacket 4 correspond exactly to the structure according to FIG. 9 and FIG. 3. The hearth 8 here consists of two rotationally symmetrical, coaxially arranged ceramic parts, of which the outer part is a hollow cylinder. The inner part is conical in the lower part, in the upper paraboloid and has a central channel with branches for guiding the gasification agent. Thanks to this stove construction, the cross section of the charging column is not radially inward but radially outward as it moves downward. In contrast to the conventional geometry, there is a parabolic / conical convex inner profile 48 of the central part of the cooker 8 with a peripheral narrowing of the throughput cross section. 49 is an outlet opening for the gasification agent in the central part of the cooker 8. 50 is a hollow cone-shaped ring body delimited by an outer cylinder and an inner cone as a counterpart, cooker end and grate. The ring body 50 is rotatably and vertically displaceably mounted (not shown) and, together with the lower part of the inner part (central body) of the cooker 8, forms an annular adjustable passage 15. The outer and the inner part of the cooker 8 is preferably with a helical channel (Coil) equipped for heating the gasification agent (not shown).

Example 1:

See Figures 1, 2, 3, 5, 6!
The plant was designed for the continuous gasification of waste wood. The gas generator essentially consisted of the cylindrical shaft-like reactor 3, the outer jacket 4 and the double-cone-shaped hearth 8 with the following dimensions: Inside diameter of the reactor shaft = 700 mm Height of the upper part of the shaft = 1600 mm Inner diameter of the outer jacket = 1600 mm Outside diameter of the outer jacket = 1800 mm Outer jacket insulation thickness = 100 mm Maximum stove inside diameter = 750 mm Minimum inner diameter of stove (narrowing) = 275 mm Opening angle of the tapered cone = 40 ^o Opening angle of the expanding cone = 60 ^o Height of the cooker = 1400 mm Total height of the shaft without loading and discharge device (active part) = 3500 mm Cross section of the helical channels = 3.2 dm²

For the shaft-like reactor 3 and the inner wall of the outer casing 4, corrosion-resistant austenitic Cr / Ni steel was used throughout as a sheet of 10 mm thickness. The same applies to the supporting sheet metal jacket surrounding the ceramic stove 8. The insulating layer 28 of the outer jacket 4 consisted of ceramic wool based on Al₂0₃. The outer cladding of the outer jacket 4 was made of low-carbon steel sheet 3 mm thick. The helical channels 21 and 22 measuring 180 mm × 180 mm were arranged according to FIG. 5 and, together with the thermally conductive intermediate wall 33, were made of 4 mm thick Cr / Ni steel sheet. The part of the reactor 3 lying above the cooker 8 was coated on the inside with 5 mm Al₂0₃ (lining 17). The ceramic hearth body 8 consisted of a high-alumina fired ramming mass, in which there was a conical helical channel 25 (spiral) of 1.2 dm 2 circular cross-section and a total of 5 turns. The average velocity of the gasifying agent air, based on normal conditions, was about 13 m / s in duct 25. The cylindrical outer wall of the hearth body 8 was protected by a heat-insulating insulating layer 29 made of ceramic wool with a radial thickness of 50 mm. The full cone 10 as a counterpart, stove top and grate had an opening angle of 60 ^o and a largest diameter of 620 mm. It was made of high-alumina ceramic and had 3 1/2 turns of a conical helical channel 23 of 0.5 dm² circular Cross section on. The velocity of the gasification agent, based on normal conditions, was about 32 m / s in channel 23. The full cone 10 could be rotated intermittently or continuously at a speed of 0.5 to 3 revolutions per minute and simultaneously or independently raised and lowered by a maximum of 200 mm. As a result, the annular passage 15 forming the grate could be adapted to the variable operating conditions.

The gas generator was also equipped with a gas-tight loading device consisting of a shaft-like structure with two loading locks 51 designed as slides. Carbon steel of approximately 10 mm thickness was used for all these parts. The same applies to the part of the container 31 adjoining the reactor for solid and liquid reaction products such as ash, slag and possibly distillation residues (charcoal, coke, semi-coke). The actual shaft-like reactor 3 was only firmly connected to the outer jacket 4 in the uppermost part, so that it could extend freely in all directions. The outer jacket 4, for its part, was supported by trusses and articulated levers on a three-legged frame made of strong steel profiles with feet.

The plant was operated as follows, with the following results (mean values) being shown: Feed material (primary fuel): old wood Primary fuel throughput: 250 kg / h Piece size of the insert: 30 - 90 mm Gas yield: 2.3 m³ / kg use Amount of gas: 575 Nm³ / h (= 160 dm³ / s) Lower heating value of the gas (moist): 3200 kJ / Nm³ Chemo-thermal performance of the gas (nominal value): 500 kW Average gas composition: C0: 18 vol .-% H₂: 8 vol .-% CH₄: 2 vol .-% C0₂: 12 vol .-% N₂ + H₂0 + 0₂: rest

Example 2:

See Figures 3, 4, 7!
A plant for the continuous gasification of lumpy, organic waste such as plastic, composite material, old cardboard etc. was provided. The gas generator consisted essentially of the same components as in Example 1 (reactor 3, outer jacket 4, stove 8) and had the following dimensions: Inside diameter of the reactor shaft = 1000 mm Height of the upper part of the shaft = 1800 mm Inner diameter of the outer jacket = 2200 mm Outside diameter of the outer jacket = 2450 mm Outer jacket insulation thickness = 125 mm Maximum stove inside diameter = 1050 mm Minimum inner diameter of stove (narrowing) = 400 mm Opening angle of the tapered cone = 45 ^o Opening angle of the expanding cone = 70 ^o Height of the cooker = 2000 mm Total height of the shaft without loading and discharge device (active part) = 4400 mm Cross section of the helical channels = 11.6 dm²

For the load-bearing components of the reactor 3 and the outer casing 4 and the hearth casing, Cr / Ni steel of 14 mm thickness was used analogously to Example 1. Ceramic wool was also used for the insulating insulating layers 28, 29 and 30. The helical Channels 21 and 22 were arranged according to FIG. 4, had a radial width of 500 mm and a height of 230 mm and consisted of 5 mm thick Cr / Ni steel sheet. The stove body made of Al₂0₃ 8 had a helical channel 25 of a total of 4 turns and a circular cross section of 3.8 dm². The average speed of the gasification agent was approximately 15 m / s. The full cone 10 mm had an aperture angle of 70 ^° and a maximum diameter of the 880th It was made of Al₂0₃ and had a conical-wavy channel 35 of 1.55 dm² circular cross-section. There were a total of 3 full trapezoidal waves. The speed of the gasification agent, based on normal conditions, was about 37 m / s in channel 35. The full cone 10 was arranged to be movable in the same way and provided with corresponding drives, as was described under Example 1.

Example 1 is referred to as regards the feeding device and the discharge of the reaction products. In accordance with the larger dimensions, a sheet thickness of 14 mm for the carbon steel used was chosen. The gas generator was supported or suspended in the frame as in Example 1.

Operating data and results of this system were as follows: Feed material (primary fuel): lumpy organic waste Primary fuel throughput: 600 kg / h Piece size of the insert: 20 - 60 mm Gas yield: 3.5 m³ / kg use Amount of gas: 2100 Nm³ / h (= 580 dm³ / s) Lower heating value of the gas (moist): 3600 kJ / Nm³ Chemo-thermal performance of the gas (nominal value): 2000 kW Average gas composition: C0: 20 vol .-% H₂: 10 vol .-% CH₄: 2 vol .-% C0₂: 11 vol .-% N₂ + H₂0 + 0₂: rest

Example 3:

See Figures 3, 5, 6, 8 (a)!
The plant was designed for the continuous gasification of compacted sewage sludge and similar waste materials originally produced in fine form. The starting material was first air-dried and then further dewatered under high pressure and pressed into oval briquettes. The basic structure of the gas generator corresponded to that of Example 1. The main dimensions were as follows: Inside diameter of the reactor shaft = 1500 mm Height of the upper part of the shaft = 2200 mm Inner diameter of the outer jacket = 3200 mm Outside diameter of the outer jacket = 3520 mm Outer jacket insulation thickness = 160 mm Maximum stove inside diameter = 1600 mm Minimum inner diameter of stove (narrowing) = 600 mm Opening angle of the tapered cone = 42 ^o Opening angle of the expanding cone = 65 ^o Height of the cooker = 2800 mm Total height of the shaft without loading and discharge device (active part) = 5600 mm Cross section of the helical channels = 28 dm²

For the main components of the reactor 3, the outer jacket 4 and the casing of the cooker 8 exposed to high temperatures, an austenitic, stabilized one was used Cr / Ni / Mo steel of 20 mm thickness is used. The heat-insulating insulation layers 28, 29 and 30 were made of high alumina ceramic fiber for operating temperatures up to 1800 ^o C. The helical channels 21 and 22 were shown in FIG. 5 arranged and passed as the intermediate wall 33 of Cr / Ni / Mo steel of 6 mm thickness. They had a radial width of 375 mm and an axial height of 750 mm. The stove made of Al₂0₃ 8 was assembled from several ring-segment-shaped sintered parts, which were interconnected by means of ceramic adhesive with a high elasticity with the interposition of thin Al₂0₃ layers of felt. The hearth 8 was broken through by a helical channel 25 of a total of 3 turns with a circular cross section of 5.6 dm 2. The average velocity of the gasification agent, based on the normal state, was approx. 25 m / s. The full cone 10 mm had an opening angle of 65 ^° and a maximum diameter of the 1300th It consisted of Al₂0₃ and had a conical-helical channel 23 with 2 1/2 turns of 2.8 dm² circular cross-section analogous to Example 1. The speed of the gasification agent, based on normal conditions, was about 50 m / s in channel 23. The movement possibilities of the full cone 10 have already been described in Example 1.

With regard to the additional construction elements, reference is made to Example 1. The sheet thicknesses were generally chosen to be approximately 18 mm for the construction material carbon steel.

The operating parameters of this gas generator are set out in the table below: Feed material (primary fuel): briquetted sewage sludge Primary fuel throughput: 1600 kg / h Piece size of the insert: 50 mm Gas yield: 3.2 m³ / kg use Amount of gas: 5100 Nm³ / h (= 1.4 m³ / s) Lower heating value of the gas (moist): 3500 kJ / Nm³ Chemo-thermal performance of the gas (nominal value): 5000 kW Average gas composition: C0: 19 vol .-% H₂: 10 vol .-% CH₄: 2 vol .-% C0₂: 11 vol .-% N₂ + H₂0 + 0₂: rest

A part of the gas flow generated was removed from the stove section according to FIG. 8 (left half of the picture) (circulating gas extraction 36) and by means of a hot gas blower 39 (0.8 m³ / s) via the pipeline 38 with heat-insulating cladding 40 into the upper part of the charging column (circulating gas return 37 ) sent back. As a result, the feed was additionally heated in descending direct current from the inside and the gasification temperature increased. Austenitic Cr / Ni steel with a wall thickness of 8 mm was used for the pipeline 38 with a cross section of 10 dm². The heat-insulating casing 40 had a thickness of 70 mm and was made of ceramic wool. The rotor of the hot gas blower 39 was composed of a heat-resistant nickel-based superalloy for operating temperatures up to 950 ^o C. For even higher temperatures can be used, where appropriate, rotors made of ceramic material such as silicon nitride, silicon carbide or ceramic composite. Since the recycle gas removal 36 takes place in the ember bed of the charging column, the gas removed is largely free of tars, tar distillates, phenols, alcohols and acetic acid, so that serious high-temperature corrosion problems need not be expected. However, if the gas contains not negligible amounts of sulfur, it must be largely nickel-free, high-chrome materials are used.

Example 4:

See Figures 3, 4, 8, 9!
A plant for the continuous gasification of lumpy raw lignite was planned. The basic components of the gas generator were the same as in Example 1. The dimensions are listed below: Inside diameter of the reactor shaft = 3000 mm Height of the upper part of the shaft = 2600 mm Inner diameter of the outer jacket = 5500 mm Outside diameter of the outer jacket = 5860 mm Outer jacket insulation thickness = 180 mm Maximum stove inside diameter = 3200 mm Minimum inner diameter of stove (narrowing) = 1600 mm Diameter of the fixed central body = 1440 mm Maximum radial width of the annular passage = 80 mm Height of the fixed central body = 3000 mm Opening angle of the tapered cone = 35 ^o Opening angle of the expanding cone = 45 ^o Height of the cooker = 5400 mm Total height of the shaft without loading and discharge device (active part) = 9000 mm Cross section of the helical channels = 120 dm²

In view of the sulfur content that is not negligible in most untreated, untreated lignites, nickel-containing materials were avoided at the critical points in the present case. The components of the reactor 3, the outer jacket 4, the casing of the Cookers 8 and the helical channels 21 and 22 were made from a ferritic, high-chromium iron base alloy with high oxidation, scale and corrosion resistance, doped with aluminum and silicon additives. The load-bearing parts were made from 30 mm sheets, the heat exchangers from 10 mm thick ones. The heat insulating layers 28, 29, 30 and 40 consisted of Al₂0₃ felt materials with a certain inherent strength. The helical channels 21 and 22 were nested according to FIG. 4, arranged analogously to Example 2. They had a square cross section of 1100 mm x 1100 mm. The cooker 8 according to FIG. 9 consisted of two parts, a peripheral part with a double-conical concave inner profile with narrowing and a cylindrical central part in the lower part and a fixed conical part in the upper part. Both parts were provided with helical channels (not shown in FIG. 9) for the gasification agent (analogous to reference numerals 25 and 23 in FIG. 3). The channel in the peripheral part of the hearth 8 had a circular cross section of 20 dm 2 and had 5 1/2 turns. The average velocity of the gasification agent in this channel was approx. 30 m / s. The hearth in the central body had a circular cross section of 12 dm² and had 4 1/2 turns. The corresponding average speed, based on normal conditions, was approx. 50 m / s. The hollow cone-shaped ring body 47 (outer cone) inserted between the two parts of the stove, rotatable and vertically displaceable, serving as counterpart, stove top and grate, was made of sintered silicon carbide in view of the requirement for high heat resistance, hardness and wear resistance.

According to FIG. 8, part of the gas flow generated, namely approx. 4 m³ / s, was removed from the hearth section in a manner similar to Example 3 (circulating gas extraction 36) and by means of a hot gas blower 39 injected via the countercurrent heat exchanger 41 as recycle gas 42 into the upper part of the feed column (recycle gas return 37). The circulating gas 42 was additionally heated by the heating gas 43 via the heat-conducting partition 44 (heat flow Q̇ with reference numeral 45). The pipeline 38 had a cross section of 40 dm 2, so that the average gas velocity, based on normal conditions, was 10 m / s. Ferritic Cr / Al steel with a wall thickness of 12 mm was used for the pipeline 38 and the heat exchanger 41. The insulating panel 40 had a thickness of 100 mm and was made of Al₂0₃ wool. The rotor of the hot gas blower 39 consisted of a heat-resistant ferritic Cr / Al / Si / Fe alloy.

The additional construction elements were made from low-carbon steel sheet with a thickness of approx. 25 mm. Reference is made to the description under Example 1.

Operating data and results for this gas generator were as follows: Feed material (primary fuel): lumpy raw lignite (dry) Primary fuel throughput: 6000 kg / h Piece size of the insert: 30 - 140 mm Gas yield: 3.6 m³ / kg use Amount of gas: 21000 Nm³ / h (= 6 m³ / s) Lower heating value of the gas (moist): 3300 kJ / Nm³ Chemo-thermal performance of the gas (nominal value): 20000 kW Average gas composition: C0: 19 vol .-% H₂: 7 vol .-% CH₄: 3 vol .-% C0₂: 10 vol .-% N₂ + H₂0 + 0₂: rest

Example 5:

See Figures 3, 5, 8, 10!
The plant was designed for the continuous degassing of lumpy hard coal. The hard coal had a content of approx. 15 to 20% volatile components. In addition to a considerable amount of semi-coke, a strong gas with a comparatively high calorific value was produced. The degassing was carried out at a maximum temperature in the oven portion of 550 ^o C. To start up the system, an excess of oxygen was initially used, ie practically gasified, in order to bring the feed to the reaction temperature. Then the oxygen supply was throttled so far that only the heat balance (heating of the feed, endothermic chemical reactions) was just balanced in the event of an oxygen deficit. This corresponded to about 10% of the amount of normal gasification air. Attention was paid to the best possible heat exchange and extensive heat recovery. The main dimensions of the gas generator were as follows: Inside diameter of the reactor shaft = 1600 mm Height of the upper part of the shaft = 2400 mm Inner diameter of the outer jacket = 3200 mm Outside diameter of the outer jacket = 3520 mm Outer jacket insulation thickness = 160 mm Stove inner diameter (peripheral part) = 1800 mm Maximum diameter of the fixed central body = 1650 mm Base diameter of the central body = 950 mm Opening angle of the conical part of the central body = 45 ^o Maximum radial width of the annular passage = 75 mm Height of the cooker (= height of the central body) = 3000 mm Total height of the shaft without loading and discharge device (active part) = 6000 mm Cross section of the helical channels = 16.6 dm²

An austenitic Cr / Ni steel of 20 mm thickness was used for the sheet metal bodies of the reactor 3, the outer casing 4 and the casing of the hearth. The heat-insulating layers 28, 29, 30 and 40 consisted of ceramic fiber mats. The helical channels 21 and 22 were arranged as shown in FIG. 5 and, including the intermediate wall 33, were made of 6 mm thick Cr / Ni steel sheet. They had a radial width of 350 mm and an axial height of 475 mm. The peripheral part of the cooker 8 consisted of several sintered full Al₂0₃ rings and had no channels. The central body of the stove made of Al₂0₃ ramming mass was provided with a helical channel for the gasifying agent (not used in the present case only used in a very reduced amount), not shown in Fig. 10, of 4 dm² circular cross section. With full carburettor operation (starting), the average speed is approx. 20 m / s. The inserted between the two oven parts of hollow cone-shaped ring body 50 (inner cone) had an opening angle of 45 ^o and consisted of sintered silicon carbide.

According to example 4, the gas generator was equipped with a device for circulating gas including heat exchanger according to FIG. 8 (reference numbers 36, 37, 38, 39, 40, 41, 42, 43, 44, 45). Here, a multiple of the gas flow generated, namely approximately 2 m³ / s, was circulated and practically heated by the heating gas 43 to the reaction temperature of 550 ^° C. via the heat exchanger 41. The pipeline 38 had a cross section of 20 dm 2, the average gas velocity was 10 m / s. For the rest, reference is made to Example 4. A common Cr / Ni steel was used as the material.

For the remaining construction elements, reference is made to Example 1. They consisted exclusively of ordinary soft carbon steel with a thickness of approx. 18 mm.

The operating data and results are listed in the following list: Feed material (primary fuel): lumpy coal Primary fuel throughput: 3300 kg / h Piece size of the insert: 20-75 mm Gas yield: 0.9 m³ / kg use Amount of gas: 3000 Nm³ / h (= 835 dm³ / s) Lower heating value of the gas (moist): 12000 kJ / Nm³ Chemo-thermal performance of the gas (nominal value): 10000 kW Average gas composition: C0: 20 vol .-% H₂: 4 vol .-% CH₄: 26 vol .-% C0₂: 3 vol .-% N₂ + H₂0 + 0₂: rest

It goes without saying that all the devices mentioned in the exemplary embodiments were equipped with the necessary monitoring and control devices such as level indicators, probes, thermocouples, pressure gauges, scales, etc. Since the equipment required for this belongs to the generally known prior art, a further detailed description is unnecessary here. It should only be pointed out that by adjusting and changing the annular passage 15, the movement of the feed column and the discharge of the reaction products, and thus the entire mode of operation with regard to the throughput of the primary fuel to be processed and the gasification or degassing temperature, vary within wide limits and that can be adapted to the respective requirements.

The invention is not restricted to the exemplary embodiments.

The process for the continuous, at least partial conversion of a solid, lumpy fuel or combustible waste material into a gaseous fuel by presorting, processing, at least partially degassing and / or at least partially gasifying in a vertical-axis shaft-like reactor 3, the starting material being in the form of a downward-sliding feed column 1 successively passes through a preheating and drying zone, a degassing zone, an oxidation zone and a reduction zone, the preheated gaseous gasification agent is injected centrally 13 into the lower part of the interior of the charging column and finally the desired gaseous fuel is produced by degassing and gasification 14 forming gaseous and vaporous reaction products in cocurrent to the feed column descending vertically downward, deflected upward and striking on the outside of the reactor wall vertically in countercurrent to the loading are directed upward, is carried out by first leading the gaseous gasification agent 2 at high speed in a helical, downward movement 6 in countercurrent to a corresponding upward helical movement 7 of the gaseous fuel generated within the jacket section 4 of the shaft-like reactor 3 and is heated, also in a helical motion 9 passed through the interior of a stove body 8 with a high heat capacity and further heated, deflected vertically upwards at the lower end of the reactor and after passing through an artificially extended section 12 with simultaneous further heating inside from below into the lower part of the loading column protruding central body is injected into the latter, the die Generated gaseous fuel 14 leaving the feed column is expelled downward through an annular passage 15, deflected and guided and cooled at high speed in countercurrent 7 to the gasifying agent 6 and by the high thermal capacity of the hearth body 8 for bridging interruptions in operation and for carrying out a specific one Intermittent processes that overlap with the continuous process are used.

In a first process variant, hard coal, lignite or wood is essentially used as the starting material and the process is carried out under a lack of oxygen in such a way that the degassing prevails and the gasification recedes and at optionally adjustable maximum temperatures of 500 to 1100 ^o C in addition to the high-quality gaseous fuel 5 from high calorific value as a further product, a high-carbon distillation residue 16 in the form of coke, semi-coke or charcoal is produced.

In a second process variant, any carbon-containing fuel or waste material is used as the starting material, and the process is carried out with sufficient oxygen so that the gasification predominates and when the latter is carried out, a maximum temperature in the charging column of at least 1200 ^° C. is set, all of which condensable higher carbon compounds such as tars, phenols, acetic acid, alcohols thermally decomposed, pyrolytically split and converted into flammable stable gases such as C0, H₂ and CH₄. Preferably, a carbon-containing fuel and predominantly a waste material which can contain Cl, F, Zn, Cd and / or Hg, as well as garbage, rubbish, sewage sludge in lumpy and / or briquetted or pelletized form or in as a starting material any other compact form, with or without a binder, and the gasification is carried out at a maximum temperature in the feed column of at least 1500 ^° C. or at least above the vaporization temperature of said toxic heavy metals under reducing conditions, the heavy metal vapors being condensed and branched off or through in a receiver Surcharge chemically bound in the feed and discharged into the slag or ash.

In a further process variant, part of the gaseous fuel generated is branched off 36 from the lower part of the charging column, optionally additionally heated with the addition of heat 45, and injected as circulating gas 42 into the upper part of the charging column for the purpose of heat transfer, 37; Heat balance continuously or intermittently H₂0 steam injected into the hottest zone of the ember bed of the charging column, the calorific value of the gaseous fuel to be generated is increased in extreme cases up to values of a strong gas.

The device for carrying out the method of at least partial degassing and / or at least partial gasification of a pre-sorted, processed solid particulate fuel or combustible waste material consists of a vertical-axis shaft-like reactor 3 with a gas-tight feed device 51 and gas-tight ash discharge or slag discharge device, and also an introduction 2 of the gaseous gasification agent and a discharge line 5 of the gaseous fuel to be produced as well as from heat exchangers, whereby a reactor shaft 3 provided at least partially with a high refractory lining 17 and a refractory ceramic cooker 8 with a narrowing downward constriction, the underside of which has a grate that can be changed as a grate Passage cross section 15 acting, vertically displaceable, rotatable ceramic counterpart is lockable, a triple cylindrical jacket 4 and a freely movable reactor shaft suspension is available, and for the supply of the gaseous gasification agent between its introduction 2 and its discharge 13 into the charging column a number of after increasing temperature, successively connected heat exchangers, which are arranged locally in a falling direction and consist essentially of cylindrical or conical basic shapes, and a ceramic central body for guiding and injecting the gaseous gasification agent from below into the lower part of the charging column, which projects comparatively deep into the latter.

In a first embodiment, the cooker 8 has a radially inward narrowing with a double-conical inner profile, the charging column in the cooker area filling the cross-section of a full circle with decreasing diameter at every level, and the ceramic central body simultaneously forms the rotatable and vertically displaceable counterpart a full cone 10 with at least one feed channel for the gaseous gasification agent.

In a second embodiment, the hearth 8 has a radially outward narrowing with a conical or paraboloid-shaped inner body, the charging column in the hearth area filling the cross-section of a circular ring with increasing inner diameter at every level, and the central body serving to guide the gaseous gasifying agent is also located Space is fixed and is part of the cooker 8, and the ceramic counterpart serving the end of the cooker has the shape of a hollow cone-shaped ring body with an outer cone 47 or an inner cone 50, is rotatable and vertically displaceable and has no channels.

The highly refractory ceramic stove body 8 is preferably equipped with cavities for guiding the gaseous gasification agent, which cavities represent at least one helical channel 25 on a virtual double cone surface or cylinder surface, the cross section of which is dimensioned such that the speed of the medium flowing through is at least 5 m / s. In an analogous sense, the central body, which serves, among other things, to guide the gaseous gasification agent, is advantageously provided with cavities in the form of at least one conical helical line 23 or at least one corrugated line 35 wound on a virtual conical surface for this purpose and is made of a ceramic material for good heat conduction high thermal conductivity and is clad on its lower end face to reduce heat loss with a heat-insulating layer 30. Advantageously, the stove body 8 is structurally designed such that it has a high heat capacity and consists of a material of high specific heat such as high-carbon ramming mass, into which a reinforcement consisting of rings and radial spokes made of a material of high thermal conductivity (such as silicon carbide) For better radial heat conduction from the ember bed of the feed is embedded in the hearth body 8 and vice versa.

The device is generally designed in an advantageous manner in such a way that the jacket section 4 of the reactor shaft 3 is equipped with a heat-insulating layer 28 forming the outer skin and that between the outer jacket 4 and the actual reactor wall 3 there is a countercurrent heat exchanger consisting of helical elements for heat transfer from the generated gaseous fuel is on the gaseous gasifying agent, such that either arranged in a layer, nested, alternately from one and the other gaseous medium in the opposite direction through which flowed at a speed of at least 3 m / s helical channels 21; 22 are present or that corresponding helical channels 21; 22 are present, those for the gaseous gasification agent outside, those for the gaseous fuel generated are inside and separated by a heat-conducting intermediate jacket 33.

Advantages of the invention:

• The process enables the highest possible energy conversion efficiency to be achieved thanks to optimal heat recovery.
• The process allows the greatest possible breadth of the process control, starting from low-temperature degassing to maximum-temperature gasification including all possible combinations, both simultaneously and intermittently in succession.
• The process provides a high purity gaseous secondary fuel and eliminates the need to install additional equipment such as gas cleaners and catalysts.
• The device can be used universally and can be used for the processing and conversion of a wide variety of primary fuels and waste materials from hard coal to wood to waste and sewage sludge.
• The device in its complete version can be operated either for the production of a weak gas or a strong gas and allows the short-term conversion of one to the other operating mode without conversion and additional devices.
• The construction of the device is simple and does not place high demands on its maintenance.
• The device can be manufactured and assembled economically according to the modular principle from the simplest, most primitive basic form to the most sophisticated version for special purposes.
• The device can be designed for a wide chemo-thermal power range of the gas from 500 kW to 20,000 kW.

Label list

1

Feeding task (solid, lumpy fuel)

2nd

Introduction of the gaseous gasifying agent (air)

3rd

Shaft-like reactor (cylindrical wall)

4th

Outer jacket of the shaft-like reactor

5

Derivation of the gaseous fuel to be generated

6

Helical guidance of the gasification agent in the jacket section

7

Helical guidance of the gaseous fuel in the jacket section (counterflow)

8th

Stove (refractory ceramic stove body)

9

Helical guidance of the gasification agent in the stove body

10th

Full cone as counterpart, stove top and grate protruding from below into the loading column (rotatable, slidable)

11

The gasification agent is fed vertically upwards in the full cone

12th

Helical guidance of the gasification agent in the full cone

13

Vertical ejection of the gasification agent from a full cone (injection in feed)

14

Gaseous fuel produced in feed, flowing vertically downwards

15

Annular, rust-forming passage between the cooker and its counterpart

16

Discharge of solid and liquid reaction products (ash, slag, distillation residue)

17th

Refractory lining of the reactor shaft

18th

Double cone-shaped concave inner profile with narrowing of the cooker

19th

Vertical feed pipe for gasifying agents carrying the full cone

20th

Rotatable, vertically displaceable shaft as a carrier and guide for the full cone

21

Helical channel (helix) for gasification agents in the jacket section

22

Helical channel (spiral) for gaseous fuel in the jacket section

23

Conical, helical channel (spiral) for gasifying agents in the full cone

24th

Outlet opening for gasifying agent in the full cone

25th

Conical, helical channel (spiral) for gasifying agents in the stove body

26

Redirection of the gaseous fuel to be generated below the hearth / grate section

27

Hollow cylindrical space between the cooker and the outer jacket for vertical guidance of the gaseous fuel

28

Thermally insulating layer of the outer jacket

29

Insulating insulating layer of the stove body

30th

Thermal insulating layer on the lower face of the full cone

31

Containers for solid and liquid reaction products (ash, slag, distillation residue)

32

External limitation of the helical channels (= inside of the outer jacket)

33

Thermally conductive intermediate jacket

34

Inlet for gasification agent in the full cone

35

Conical-wavy channel for gasifying agents in the full cone

36

Circulation gas extraction from the lower part of the charging column

37

Return gas circulation in the upper part of the charging column

38

Pipe for recycle gas

39

Hot gas blower for circulating gas

40

Insulating cladding

41

Counterflow heat exchanger for recycle gas

42

Recycle gas

43

Heating gas (burner gas, high-temperature exhaust gas)

44

Heat-conducting partition of the heat exchanger

45

Heat flow Q̇

46

Outlet opening for gasification agent in the central conical part of the stove body

47

Hollow-conical ring body (outer cone) as counterpart, stove top and grate (rotatable, slidable)

48

Parabolic / tapered convex inner profile of the central part of the hearth with peripheral narrowing

49

Outlet opening for gasification agent in the central part of the stove body

50

Hollow-conical ring body (inner cone) as counterpart, stove top and grate (rotatable, slidable)

51

Gas-tight loading locks (sliders)

Claims (12)

Process for the continuous, at least partial conversion of a solid, lumpy fuel or combustible waste material into a gaseous fuel by presorting, processing, at least partially degassing and / or at least partially gasifying in a vertical-axis shaft-like reactor (3), the starting material in the form of a downward sliding Feed column (1) successively passes through a preheating and drying, a degassing, an oxidation and a reduction zone, the preheated gaseous gasifying agent is injected centrally (13) into the lower part of the interior of the charging column and the gases generated by degassing and gasification, finally, the gaseous and vaporous reaction products forming the desired gaseous fuel (14) are passed in a cocurrent to the charging column descending vertically, diverted upward and vertically in countercurrent on the outside of the reactor wall r feed column are directed upwards, characterized in that the gaseous gasifying agent (2) at high speed initially in a helical, downward movement (6) in countercurrent to a corresponding upward helical movement (7) of the gaseous fuel produced within the Mantle section (4) of the shaft-like reactor (3) is guided and heated, also in a helical movement (9) through the interior of a stove body (8) with a high heat capacity and further heated, deflected vertically upwards at the lower end of the reactor and after passing through an artificially extended route (12) with simultaneous further heating inside from below into the lower part of the Central body (10) projecting into the charging column is injected into the latter, and that the gaseous fuel (14) leaving the charging column is expelled downward through an annular passage (15), deflected and guided at high speed in countercurrent (7) to the gasification agent (6) and is cooled, and that the high heat capacity of the hearth body (8) is used to bridge interruptions in operation and to carry out intermittent processes which require a certain temperature program and are superimposed on the continuous process. A method according to claim 1, characterized in that essentially hard coal, lignite or wood is used as the starting material and that the process is carried out in such a way that the degassing prevails and the gasification recedes and that at optionally adjustable maximum temperatures of 500 to 1100 ^o C in addition to high-quality gaseous fuel (5) of high calorific value as a further product a high-carbon distillation residue (16) is produced in the form of coke, semi-coke or charcoal. A method according to claim 1, characterized in that any carbon-containing fuel or waste material is used as the starting material and that the process is carried out in such a way that the gasification predominates and that when the latter is carried out, a maximum temperature in the charging column of at least 1200 ^° C. is set is such that all condensable higher carbon compounds such as tars, phenols, acetic acid, alcohols thermally decompose, pyrolytically split and into flammable stable gases such as C0, H₂, CH₄ and fiber are converted. A method according to claim 3, characterized in that the starting material is a carbon-containing fuel and predominantly a waste material which can contain Cl, F, Zn, Cd and / or Hg, as well as garbage, rubbish, sewage sludge in lumpy and / or in briquetted or pelletized form or in any other compacted form with or without a binder and that the gasification is carried out at a maximum temperature in the feed column of at least 1500 ^o C or at least above the vaporization temperature of said toxic heavy metals under reducing conditions and the heavy metal vapors condensed in a template and branched off or chemically bound by addition in the feed and discharged into the slag or ash. A method according to claim 1, characterized in that a part of the gaseous fuel produced branches off (36) from the lower part of the charging column, optionally additionally heated with the addition of heat (45) and as circulating gas (42) into the upper part of the charging column for the purpose of heat transfer is injected (37) and that, in order to compensate for the heat balance, H₂0 steam is injected continuously or intermittently into the hottest zone of the ember bed of the charging column, in such a way that the calorific value of the gaseous fuel to be generated is increased in extreme cases up to values of a strong gas. Device for carrying out the method of at least partial degassing and / or at least partial gasification of a pre-sorted, processed solid particulate fuel or combustible waste material according to claim 1, the device comprising a vertical-axis shaft-like reactor (3) with a gas-tight feed device (51) and a gas-tight ash discharge or slag discharge device, further comprising an introduction (2) of the gaseous gasification agent and a discharge line ( 5) of the gaseous fuel to be produced and of heat exchangers, in such a way that an at least partially provided with a high refractory lining (17) reactor shaft (3) and a downwardly narrowing constricting refractory ceramic stove (8), the underside with an as Grate with a variable passage cross-section (15) acting, vertically displaceable, rotatable ceramic counterpart is lockable, a triple cylindrical jacket (4) and a freely movable reactor shaft suspension is provided, characterized in that for the supply of the gaseous gas Between the introduction (2) and the ejection (13) into the charging column, a series of heat exchangers consisting of cylindrical or conical basic shapes, arranged one after the other in a falling direction and arranged in a falling direction, is provided, and that a ceramic central body for guiding and injection of the gaseous gasification agent is provided from below into the lower part of the charging column, which projects comparatively deep into the latter. Apparatus according to claim 6, characterized in that the hearth (8) has a radially inward narrowing with a double-conical inner profile, such that the charging column in the hearth area has the cross-section of a full circle at every level fills with a decreasing diameter, and that the ceramic central body simultaneously represents the rotatable and vertically displaceable counterpart in the form of a full cone (10) with at least one feed channel for the gaseous gasification agent. Apparatus according to claim 6, characterized in that the hearth (8) has a radially outward narrowing with a conical or paraboloidal inner body, in such a way that the charging column in the hearth area fills the cross-section of a circular ring with increasing inner diameter at every level, and that the central body serving to guide the gaseous gasification agent is fixed in space and is part of the cooker (8), and that the ceramic counterpart serving to close the cooker is in the form of a hollow-cone-shaped ring body with an outer cone (47) or an inner cone (50), rotatable and vertically displaceable and has no channels. Apparatus according to claim 6, characterized in that the highly refractory ceramic hearth body (8) is equipped with cavities for guiding the gaseous gasification agent, which represent at least one helical channel (25) on a virtual double cone surface or cylinder surface, the cross section of which is dimensioned in this way, that the velocity of the medium flowing through is at least 5 m / s. Apparatus according to claim 6, characterized in that the central body, which is used, among other things, to guide the gaseous gasification agent, has cavities in the form of at least one conical helical line (23) or at least one for this purpose is provided on a virtual cone-shaped surface of the corrugated line (35) and that for good heat conduction it consists of a ceramic material with high thermal conductivity and is clad on its lower end face to reduce heat losses with a heat-insulating layer (30). Apparatus according to claim 6, characterized in that the hearth body (8) is structurally voluminous in such a way that it has a high heat capacity and that it consists of a material of high specific heat such as high-carbon ramming mass, into which a reinforcement consisting of rings and radial spokes from a material of high thermal conductivity (such as silicon carbide) for the purpose of better radial heat conduction from the ember bed of the feed is embedded in the hearth body (8) and vice versa. Apparatus according to claim 6, characterized in that the jacket section (4) of the reactor shaft (3) is equipped with a heat-insulating layer (28) forming the outer skin and that between the outer jacket (4) and the actual reactor wall (3) is a helical Elements of existing countercurrent heat exchangers for heat transfer from the generated gaseous fuel to the gaseous gasification agent, such that helical channels either arranged in a layer, nested, alternately flowed through by one and another gaseous medium in opposite directions at a speed of at least 3 m / s (21 ; 22) are present or that corresponding helical arranged in two layers Channels (21; 22) are present, those for the gaseous gasification agent outside, those for the gaseous fuel generated inside and separated by a heat-conducting intermediate jacket (33).

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