Method and device for adjusting the filling level of a floating bed reactor

Abstract

To provide a method for adjusting or defining a filling level or filling height of a bed held in a suspended state (floating state) at a carbonaceous material gasifier, especially a floating bed reactor.SOLUTION: In a floating bed reactor 300 type carbonaceous material gasifier that converts biomass and / or coke K into a product gas 403, a downwardly tapered floating bed reactor equipped with a lower inflow opening 301 is prepared, a raw material is introduced downward and a gasifying agent V for a gas is introduced upward. Considering the material properties of the biomass and / or the coke so that a stable fixed bed held in the suspension state is produced in the floating bed reactor, a flow rate of the gasifying agent is adapted to a shape of a flow cross section of a conical reactor. Height of an upper boundary layer of the fixed bed in the reactor is adjusted by extracting the gas together with particles from an extraction pipe 303, protruding downward into a reaction chamber, that is provided in a reactor ceiling 302, and a position of the extraction pipe determines a vertical position of the upper boundary layer of the floating bed.SELECTED DRAWING: Figure 2

Description

[Technical field]

[0001] The present invention relates to an apparatus and method for adjusting the loading level or loading height in a gasifier for carbonaceous materials, in particular in a floating bed gasifier or reactor, and in particular to a method for discharging particles from a floating bed gasifier, which allows the loading level or loading height of the bed held in suspension to be adjusted or defined.

[0002] In the context of this application, a floating bed or floating fixed bed is a fixed bed that acts against gravity and is suspended by the incoming gas flow, i.e. suspended from the gas inlet. In contrast to a fluidized bed, it contains bulk material capable of transmitting shear stresses and therefore has an internal friction angle of >>0°, preferably 35° to 50°. Furthermore, a floating fixed bed is considered to be a stable fixed bed operated below its bulk-mechanical fluidization limit and thus kept in suspension. Operating a floating fixed bed above its fluidization limit leads to instability and therefore changes it from a floating fixed bed to a fluidized bed. [Background technology]

[0003] DE 10 2007 012 452 A1 discloses a gasifier for organic matter in a floating bed. The floating bed gasification is described as a staged gasification process in which the carbonaceous material is preferably pyrolyzed or carbonized to a certain coke, and then the resulting coke is gasified as completely as possible in a floating bed reactor together with the pyrolysis gases to the so-called product gas. The product gas is also called lean gas or synthesis gas. Such a floating bed reactor comprises a substantially frustoconical widening region adjacent to the inlet, which merges into a cylindrical section with an outlet at the end. This body contains a fixed bed formed by the coke, which is kept in suspension by the inflow of a gasifying agent and is supplied from a previous pyrolysis process. The coke is kept in suspension in an elevated, lifted or floating position by suitable introduction and flow regulation of a gasifying agent such as air, and is continuously converted or gasified into product gas.

[0004] In order to adjust the filling level, i.e. the height, of the floating bed in fixed floating bed gasifiers or the position of the upper boundary layer of the floating bed, discharge units in the form of an overflow in the upper region of the floating bed reactor are known, which are shown for example in figure 5 of WO 2008 / 110383 and will be described in more detail below with reference to figure 1 of the present application.

[0005] This known discharge unit or overflow is used in particular for removing undesirable substances such as ash, which are only reduced to a limited extent or insufficiently or not reduced in a short enough time, and are therefore converted into their gaseous form. Reference is further made to EP 2 886 190 A1, which discloses how impurities with a higher density than coke, such as stones or metal parts, are removed from the material flow below the floating bed reactor.

[0006] The overflow in WO 2008 / 110383 is essentially gravitational, i.e. the heavier particles fall downwards so that the lighter materials, which are kept in suspension, are not yet discharged and therefore only discharged when they clump together into larger particles or agglomerates.

[0007] EP 2 862 914 A describes a system with lances combined with sensors at the top of the floating bed reactor. These lances can be used to introduce additional gasifying agent into the upper non-load-bearing layer of the floating bed. The term non-load-bearing layer means a layer in which lateral forces in the bed are no longer relevant to maintain a stable floating fixed bed. Furthermore, EP 2 862 914 A describes that overflow of the floating bed reactor can be prevented if a filling level reading is provided at its upper end by a sensor. As an example of a filling level sensor, for example a radar sensor is given. [Prior art documents] [Patent documents]

[0008] [Patent Document 1] German Patent Application Publication No. 102007012452A1 [Patent Document 2] European Patent Application Publication No. 2886190 [Patent Document 3] International Publication No. 2008 / 110383 Brochure [Patent Document 4] European Patent Application Publication No. 2862914 Summary of the Invention

[0009] It is an object of the present invention to provide a method and a corresponding device for reliable and safe long-term operation of a floating bed reactor which allows substantially simpler control or regulation. This object is achieved by means of the features of the independent claims. Further preferred embodiments of the invention are set forth in the dependent claims.

[0010] The inventors of the present invention have found that removing material from the top of the floating bed has advantages in terms of stability and efficiency. According to the present invention, it is preferably possible to largely omit sensors and their associated circuits. For example, materials that cannot be further reduced, such as ash, can be easily removed from the top of the floating bed by extraction to adjust or control the top fill level in the floating bed reactor.

[0011] Preferably, the method according to the invention is used in combination with an impurity removal method as described in EP 2 886 190. In other words, particles that are denser than the coke material, such as stones, pebbles, sand grains, slag, nails, screws and / or other metal particles, are preferably removed from the material stream at an early stage, thus preferably preventing these impurities from accumulating in the floating bed in the first place.

[0012] First of all, the invention relates in particular to a method by which the filling level can be adjusted or controlled in a floating bed reactor type gasifier for carbonaceous materials, in which biomass and / or coke are converted into product gas (lean gas or synthesis gas). First, an essentially conical, downwardly tapering floating bed reactor is provided, which has an upper reactor ceiling or upper reactor cover and an inlet opening at the lower end. According to the invention, the biomass and / or coke K in the form of a gas stream is transported through this inlet opening from bottom to top into the floating bed reactor. Furthermore, a gaseous gasifying agent V is also introduced into the floating bed reactor from bottom to top, i.e. against gravity. The coke K can be oriented, for example, horizontally, vertically or at any angle between them, in the form of perfect flow, and can then be transported into the floating bed reactor together with the gasifying agent V, which is directed from bottom to top. This is advantageous, for example, with regard to the separation of heavy solids such as stones or metal particles. Since the method according to the invention is essentially concerned with the discharge of lean gases at the top of the floating bed reactor, the method according to the invention is not limited to the specific embodiment of introducing coke K and gasifying agent V. The crucial point is that a fixed bed is formed in the reactor, preferably at least in the conical part of the reactor, which is kept in suspension. This bed is preferably at an elevated position or spaced apart from the location of the inlet opening.

[0013] The floating bed extends between a lower boundary layer and an upper boundary layer in the reactor, the spacing between which defines the thickness or depth of the floating bed and the vertical location of the upper boundary layer, hereinafter referred to as the packing level.

[0014] In the equilibrium operation of the floating bed, the gasifying agent is introduced in an amount just sufficient to keep the amount of coke in the fluidized bed reactor constant. This balances the cracking of the coke with its continuous conversion to product gas and the introduction of new bio-coke fractions. Due to the generally non-uniform composition of the biomass fed, as well as measurement tolerances in the loading of the biomass and the introduction of the gasifying agent, this equilibrium operation may vary over time, so that within narrow limits, the floating bed is intermittently operated in accumulation and cracking modes.

[0015] During the build-up operation, more coke is introduced into the reactor than is cracked at that time. This increases the amount of gasified coke in the reactor. This causes a region in the floating bed reactor to be continuously replaced by new material, and the excess material from this region is taken up towards the top in the floating bed. Thus, the filling level in the reactor continues to rise. To prevent the reactor from overflowing, the invention is equipped with at least one withdrawal pipe at its upper end, which allows the material or particles of the floating bed to be withdrawn, and thus the filling level can be adjusted. Preferably, this allows the filling level to be measured from above as the filling height in the floating bed reactor, and this level can be kept substantially constant.

[0016] Above the conical section of the reactor, a substantially cylindrical section of substantially constant diameter may also be provided. Here, a bed held in suspension above the conical section may also occur in the cylindrical section. Essential for the formation of a floating bed is the tapered (downwards) or divergent (upwards) shape of the reactor and the flow rate of the gasifying agent depending on the material properties of the biomass and / or coke. Here, the flow rate is adapted to the shape of the flow cross section of the conical reactor, taking into account the material properties of the biomass and / or coke, so that a bed held in suspension is formed. It has been found that the flow rate can be easily experimentally adapted to the conical shape and the material properties to achieve the desired floating bed. On the other hand, it has also been found that theoretical descriptions or empirical parameterizations to describe floating beds are not possible or are not possible with sufficient accuracy so far. However, the skilled person will be able to easily form a corresponding fixed bed held in suspension by simply varying the flow rate.

[0017] A fixed bed kept in suspension is fundamentally different from known fixed beds, which are usually placed on a grid, and also from fluidized beds, in which the particle velocities are high. Like conventional fixed beds, the floating fixed bed according to the invention has a "solid bed", i.e. the particles of the bed are practically immobile. However, a bed kept in suspension does not rest on anything, in particular on a grid or other mechanical structure, but is kept in suspension by the gas flow. The conical shape of the reactor is therefore not a rest for the bed, but merely a lateral support. A bed kept in suspension can therefore be described, for example, by the particle velocity of the solids.

[0018] Preferably, the particle velocity in the region of the fixed bed is close to 0 m / s. However, as the fixed bed shrinks over time, as would be the case over a long period of time, there is a (very) slow movement of particles (preferably upwards) within the bed, but the particle velocity of this movement is preferably less than 1 m / s, preferably less than 0.5 m / s, preferably less than 0.2 m / s, preferably less than 0.05 m / s. Preferably, this particle velocity refers to the average value of all particles in the bed.

[0019] On the other hand, the velocity of the gas particles or gas flowing through the fixed bed while keeping it in suspension is preferably very high, preferably higher than 2 m / s, preferably higher than 5 m / s, preferably higher than 10 m / s. Instead of the absolute values ​​of the particle and gas velocities of the bed, the relative ratio of these two velocities can also be used to characterize the floating bed. For example, the ratio of gas velocity / particle velocity is preferably >10, preferably >50, preferably >100. By comparison, for a fluidized bed gasifier, the value of this ratio will be of the order of 1.

[0020] A bed maintained in suspension may also be characterized, for example, by the fact that there is no significant axial mixing of the solids, i.e., there is virtually no mixing from bottom to top or top to bottom within the fixed bed. Rather, during gasification, the particles in the fixed bed move very slowly from the bottom, where they are introduced and initially form a support layer, towards the top until they are withdrawn in accordance with the present invention. There is virtually no movement of solid particles counter-current to the gas flow, i.e. downward.

[0021] A floating bed can further be described by the fact that shear forces are transmitted between the solid particles in the bed and that the internal friction angle that arises is clearly >0°, preferably >10°, preferably >20°, preferably >30°, preferably >35°, preferably <60°, for example 35° to 50°.

[0022] The fixed bed held in suspension in the floating fixed bed reactor preferably has as a further property a bulk-mechanical horizontal load ratio lambda (λ) value according to the invention between 1 and 0, i.e. neither 1 (liquid) nor 0 (solid). The λ value is particularly preferably between 0.3 and 0.6. For example, in the book "Pulver und Schuettgueter: Fliesseigenschaften und Handhabung" ("Powder and Bulk Materials: Flow Properties and Handling") by Dietmar Schulze, published by Springerverlag on December 12, 2008, the λ value is defined as follows:

[0023] The bulk material element in a container filled with bulk material has a positive normal stress σ v >0 (compressive stress) acts in the vertical direction, i.e., from both above and below. If we were to assume that the bulk material behaved like a Newtonian liquid at rest, the stress acting in the horizontal direction should be the same as that acting in the vertical direction (and in all other directions). However, bulk materials behave in many ways completely differently from liquids, so considering an analogy between bulk materials and liquids often leads to erroneous conclusions. Due to a vertical load in the horizontal direction, the bulk material experiences a normal stress σ v Smaller stress σ h Stress σ h and σ v The ratio of σ to λ is defined as the horizontal load ratio λ (also called the horizontal stress ratio or K internationally): λ = σ h / σ v .

[0024] The method according to the invention is particularly advantageous for adjusting the height or position of the upper boundary layer or edge of the fixed bed or the upper region of the fixed bed in the reactor. In particular, the gas together with the particles is withdrawn from the reactor by at least one withdrawal pipe penetrating the reactor ceiling (or reactor cover) and projecting downwards into the reactor chamber or reactor volume. Preferably, the length of the withdrawal pipe determines the position of the upper edge or upper boundary layer of the floating bed in the reactor.

[0025] According to the invention, the at least one pipe may be arranged substantially in the center of the cover. In other words, the pipe and the reactor are preferably arranged concentrically. According to the invention, the pipe may also be arranged in the cover laterally offset from the center of the reactor, i.e. laterally offset from the central axis of the reactor. In addition, it may be advantageous to arrange several pipes in the reactor cover for extraction. All or some of the pipes may extend to the same or different depths inside the reactor.

[0026] Multiple pipes extending to different depths in the reactor may be advantageous, for example, when adjusting for different filling levels inside the reactor, for example only one of the multiple pipes may be used for suction, whereby the filling level is adapted to the length of each pipe used.

[0027] According to another embodiment of the invention, at least one pipe may be adjustable or slidable so that the length of the pipe extending into the reactor can be adjusted. This can be advantageous, for example, when the reactor is operated with very different biomasses over time, causing the floating bed height to change.

[0028] According to the present invention, the terms "floating bed" and "floating fixed bed" are used synonymously. Thus, the terms "floating bed gasifier", "floating bed reactor", "floating fixed bed gasifier" or "floating fixed bed reactor" as well as the terms "reduction unit with a floating / fixed bed formed therein" or "reduction unit with a bed / fixed bed held in suspension" are used synonymously. In other words, a floating bed can be described as a layer / bed formed as a fixed bed in a gasification reactor, which is elevated from the lower inlet region, i.e. it actually "floats" above the gas flow in the true sense of the term, similar to the floating bed gasification according to the disclosures of DE102007012452A1 or WO2008 / 110383. In particular, the present invention makes general reference to the basic principles of the floating bed gasifier disclosed in said publications.

[0029] The process according to the invention is therefore characterised in that, for example, at the inflow of gasifying agent, the carbonised biomass, which is a fixed bed, is kept in suspension in a floating bed reactor, while the material present above the floating bed is substantially withdrawn from the top of the reactor.

[0030] However, the floating bed gasifier according to the invention is not limited to the methods for producing gas from biomass described in the abovementioned publications. Instead, the floating bed gasification method according to the invention can be applied to any appropriately treated carbonaceous solid material source. For example, dried sewage sludge can also be converted without an upstream pyrolysis unit, since its composition is dominated by carbonaceous materials. In principle, the same applies to the use according to the invention of externally produced coal or coke. It is therefore not absolutely necessary for the operation of the floating bed reactor that the fed biomass is already largely carbonized. However, in the following, only the feeding of coke is mentioned.

[0031] According to the invention, the solid residue that has not been converted to gas can be removed substantially continuously without adversely affecting the amount of gas produced, its quality, or the overall efficiency of the plant.

[0032] According to the present invention, the produced lean gas is discharged from the floating bed reactor together with the particles, but it is preferred to filter out the discharged particles by a filtration device in order to use the lean gas later.

[0033] In accordance with the present invention, by supplying additional gas to the top of the bed held in suspension using a lance, it is possible to have a much greater influence or control over the characteristics of the exiting gas stream. In particular, by introducing additional gas and withdrawing particles, it is possible to affect both the quantity and characteristics of the gas stream exiting the reactor. [Brief description of the drawings]

[0034] [Figure 1] FIG. 1 is a schematic diagram of a known reduction unit according to WO 2008 / 110383; [Diagram 2] FIG. 2 is a schematic diagram of a reduction unit equipped with a discharge device according to the present invention of the extraction pipe type. DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

[0035] Further features and advantages of embodiments of the invention are explained in more detail below with reference to examples and with the aid of the drawings, in comparison with known devices.

[0036] FIG. 1 shows a floating bed gasifier 3 known from WO 2008 / 110383 and the corresponding EP 2 129 749 B1. With regard to the pyrolysis unit 1, the oxidation unit 2, the lift screw 4, the outlet 5, the gas nozzle 6 and the nozzle units 7 and 8 shown, reference is made to the disclosure of WO 2008 / 110383, since the device according to the invention essentially relates to this floating bed gasifier 3. In the known floating bed gasifier 3, a discharge unit or overflow 32 (see FIG. 1 "Product ash discharge") is shown, which is attached to the known floating bed gasifier 3 before or below the gas outlet 31 so that material can be removed from the floating bed gasifier 3. This discharge unit 32 can be arranged, at least in places, in an annular manner around the floating bed gasifier. The discharge unit or overflow 32 is in particular used to remove undesirable substances such as ash or foreign bodies from the floating bed gasifier 3. Such substances may be reduced to a limited extent, insufficiently, or not in a short enough time, and therefore converted to gaseous form. These undesirable substances are discharged gravimetrically, for example from a predetermined or adjustable filling level of the floating bed and / or via a mechanical system (overflow), to a discharge unit.

[0037] The reduction unit or floating bed gasifier 3 preferably has at least one outlet 31 for discharging the generated combustible gas (synthesis gas), also called the gas outlet 31 ("product reducer"). At the gas outlet 31 of the floating bed gasifier 3, the gas flow of the generated synthesis gas leaves upwards, i.e. against gravity. After optional steps, such as cooling, for example in a heat exchanger, and / or purification, this gas can be fed to a gas storage tank or a combustion engine and / or used for other purposes. In this embodiment according to the prior art, the upper part of the floating bed gasifier is conically tapered, so that the generated light gases are directed to the gas outlet as if coming out of a funnel.

[0038] FIG. 2 shows a floating bed gasifier 300 of the present invention in which a floating bed 402 is formed. To form the floating bed 402, the lower part of the floating bed gasifier 300 is expanded substantially conically upwards, similarly or identically to the prior art. In this embodiment, the biomass and / or coke K is transported substantially horizontally from the left under the inlet opening 301 of the reactor by a transport device. This can be done, for example, by a spiral or screw conveyor for demand-based metering. In this figure, the gaseous gasifying agent V is introduced from the right side, so that the biomass / coke in the inlet gas stream of the gasifying agent V is transported substantially vertically upwards, i.e. substantially against gravity, through the inlet region 301 of the reactor into the reactor 300. However, the present invention is not limited to this particular introduction form, and all possible embodiments for forming the floating bed are applicable. For example, to separate undesirable impurities at an early stage, it is advantageous if the gasifying agent V flows from below (vertically) and the biomass meets the gas flow of the gasifying agent V rising vertically transversely, i.e. horizontally, or at any angle between 0 and 180° to the vertical, preferably at an angle between 45° and 135°, more preferably at an angle between 70° and 110°, preferably at an angle essentially vertical (90°).

[0039] The top of the floating bed gasifier 300 according to the present invention differs from the floating bed gasifier 3 shown in Figure 1 in that the cover (ceiling) 302 is oriented substantially horizontally, rather than being an upwardly tapered cone. The generated synthesis gas is extracted through a pipe 303 that runs from top to bottom through the cover 302 into the interior of the gasifier 302, so a conically tapered cover is not necessary. In other words, no upward gas funnel is required, since the gas is extracted from the interior of the gasifier 300.

[0040] According to the invention, the synthesis gas is not only driven upwards by the heat flowing upwards, but is actively extracted through the pipe 303, so that the part of the gas that accumulates above the lower end of the pipe 303 but below the cover 302 is also effectively extracted (see arrow in FIG. 2). In addition, material can also be actively extracted from the top of the formed floating bed. This has the decisive advantage that the upper filling level can be effectively and to some extent automatically controlled or adjusted, depending on the length of the pipe 303 that protrudes into the gasifier. The upper edge of the bed that is kept in suspension (upper boundary layer) is preferably approximately at the same height in the reactor as the lower end of the pipe 303. It should be noted here that this is not shown exactly in FIG. 2, the lower end of the pipe 303 being drawn too high.

[0041] That is, in order to allow more precise control of the filling level in the floating bed gasifier 300 as well as the coal production, according to the present invention, an extraction device is provided at the top of the floating bed gasifier 300 (not shown). Preferably, a pipe 303 is provided at the top of the floating bed gasifier 300 to allow the particles to be extracted from the surface or interface 410 of the formed floating bed 402.

[0042] This simple extraction has the advantage that it can be performed without complex filling level sensors and associated control means, for example. This controlled release of fines can, for example, further increase the stability of the floating fixed bed. A lance in the upper region can also be omitted, resulting in a simple but stable control / regulation of the floating bed.

[0043] According to the invention, the produced gas is withdrawn together with solid particles, which are preferably filtered out in a filtration system (not shown). After suitable cooling and, optionally, energy recovery and purification steps, the produced gas can then be used to operate a device such as a thermal power engine. Alternatively or additionally, the produced gas can be used in further purification processes (e.g., for biofuel production) or can be utilized, for example, in a fuel cell.

Claims

1. A method for adjusting the fill level of a gasifier for carbonaceous materials in the form of a floating bed reactor (300) in which biomass and / or coke (K) is converted into product gas (403), comprising the steps of: Providing a substantially downwardly tapered conical floating bed reactor (300) having a reactor ceiling (302) and a lower inlet opening (301), introducing biomass and / or coke (K) from below into the floating bed reactor (300) through the inlet opening and introducing a gaseous gasifying agent (V) upward, thereby forming a floating bed (402) held in suspension at a position higher than the position of the inlet opening inside the conical floating bed reactor (300); wherein the flow rate of the gaseous gasifying agent (V) introduced together with the biomass and / or coke (K) is adapted to the shape of the flow cross section of the conical floating bed reactor (300) taking into account the material properties of the biomass and / or coke so that a stable bed held in suspension is formed in the floating bed reactor (300); Here, the adjustment of the filling level of the floating bed, which is maintained in a suspended state inside the floating bed reactor (300), Gas is withdrawn together with the particles through a withdrawal pipe (303) in the ceiling (302) of the floating bed reactor, said pipe projecting downwards into the reactor chamber, the position of the lower end of said withdrawal pipe (303) determining the position above the floating bed in the floating bed reactor (300).

2. 2. The method according to claim 1, wherein the floating bed (402) has a lower boundary layer (400) and an upper boundary layer (410) formed or extending between these boundary layers, the vertical position of the upper boundary layer (410) being at substantially the same level as the lower end of the withdrawal pipe (303) within the floating bed reactor (300).

3. 3. The method of claim 1 or 2, wherein the lower boundary layer (400) of the floating bed (402) is maintained in suspension and does not rest on a grid.

4. 4. The method according to any one of claims 1 to 3, wherein the withdrawn particles are filtered out by a filtration device after being withdrawn from the floating bed reactor (300).

5. 5. The method according to claim 1, wherein the velocity of the particles forming the bed is approximately 0 m / s in the region of the floating bed (402), while the velocity of the gas flowing through the bed kept in suspension is clearly >> 0 m / s.

6. 6. The process according to any one of claims 1 to 5, wherein there is substantially no axial mixing of solids in the fixed bed reactor with floating bed.

7. 7. The method according to any one of claims 1 to 6, wherein the shear forces transmitted between the solid particles in the floating bed are applied such that the resulting angle of internal friction is clearly >0°, preferably >10°, preferably >20°, preferably >30°, preferably >35°, preferably <60°, for example between 35° and 50°.

8. 8. The method according to claim 1, wherein the fixed bed kept in suspension in the floating bed reactor is characterized by a bulk-mechanical horizontal load ratio λ having a value between 1 and 0, i.e. neither 1 (liquid) nor 0 (solid), particularly preferably between 0.3 and 0.6, the bulk-mechanical horizontal load ratio λ being expressed as the ratio of stresses σh and σv, where σh represents the horizontal stress on the floating bed 402 when the floating bed is a liquid and σv represents the vertical stress on the floating bed 402 when the floating bed is a bulk material.

9. 9. The method according to any one of claims 1 to 8, wherein the reactor ceiling (302) is substantially flat and horizontal.

10. 10. The process according to any one of claims 1 to 9, wherein additional gas is supplied by a lance to the upper part, preferably the upper third, of the bed held in suspension, so that the introduction of said additional gas and the withdrawal of particles can influence the amount of gas flow leaving the reactor.

11. An installation for carrying out the method according to any one of claims 1 to 10, comprising: A substantially conical floating bed reactor (300); means for feeding biomass and / or coke (K) and gasification agent (V) from bottom to top into said floating bed reactor; a withdrawal device for withdrawing product gas and particles from the floating bed reactor (300); Equipped with The equipment is characterized in that the withdrawal device has at least one pipe (303) installed in the ceiling (302) of the floating bed reactor (300), the pipe protruding into the interior of the floating bed reactor (300), and the product gas and particles are withdrawn from the floating bed reactor through the pipe.

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