EP2451904A2

EP2451904A2 - Reactor for generating a product gas by allothermic gasification of carbonaceous raw materials

Info

Publication number: EP2451904A2
Application number: EP10728178A
Authority: EP
Inventors: Michael Hofmeister; Stefan Aniol; Georg Gallmetzer
Original assignee: Highterm Research GmbH
Current assignee: Highterm Research GmbH
Priority date: 2009-07-10
Filing date: 2010-06-22
Publication date: 2012-05-16
Also published as: US20110300027A1; CN102307972A; WO2011003731A2; CA2749822A1; DE102009032524B3; BRPI1008521A2; WO2011003731A3

Abstract

The invention relates to a reactor for generating a product gas by allothermic gasification of carbonaceous raw materials, comprising a pressure-charged reformer reactor for gasification of the carbonaceous raw materials, a feed line for feeding carbonaceous raw materials and ancillary materials for gasification into the reformer reactor, a combustion chamber for generating the heat required for the allothermic gasification, the combustion chamber being thermally coupled to the reformer reactor, and a pneumatic conveyor device for removing particulate gasification residue and raw gas from the reformer reactor and for feeding the particulate gasification residue into the combustion chamber, having a gas filter for separating out the particulate gasification residue from the raw gas and a pressure lock having a high-pressure side and a low-pressure side, the gas filter comprising a discharge line for product gas and a discharge line for solid particles. The reactor is characterized in that the gas filter and the pressure lock are separate components, and in that the gas filter discharge line for solid particles is connected to the high-pressure side of the pressure lock.

Description

description

Reactor for producing a product gas by allothermic gasification of carbonaceous feedstocks

The present invention relates to a reactor for producing a product gas by allothermic gasification of carbonaceous feedstocks according to the preamble of claim 1,

In particular, the present invention relates to such a reactor in which biogenic starting materials (biomass), such as harvest waste, woodchips or energy crops, ie plants such as miscanthus, which are cultivated and cultivated specifically for energy use, are reacted as carbonaceous feedstocks. In particular, the reactor according to the invention is used to produce product gas (synthesis gas), a mixture of carbon monoxide and hydrogen, with a calorific value of at least 8,000 to 10,000 kJ / m ³ , ie with a calorific value above that of lean gas of about 3,500 to 7,000 kJ / m ³ (for comparison: the calorific value of gas produced under the influence of microorganisms from organic substances is between 21,000 and 25,000 kJ / m ³ ). The product gas thus obtained may be supplied for further use to a gas engine or a gas turbine to be burned therein with an efficiency of about 35-40%.

The process of allothermic - that is, in the sum of endothermic - water vapor reforming of biomass generally takes place in three sub-processes: drying, pyrolysis (splitting or "cracking" of long-chain organic compounds substantially, ie apart from the oxygen contained in the biomass, under Oxygen exclusion, excess air ratio λ = 0) and (steam) reforming, whereby the product gas is produced at the end of the process All three partial processes take place simultaneously in a fluidized-bed reactor of a so-called heat pipe reformer the stoichiometric gasification (0 <λ <1) with low oxygen supply and the combustion (λ> 1) with optimum oxygen supply delimited. The pyrolytic decomposition of biomass under the action of heat and the formation of air produces gaseous (pyrolysis gas) and liquid (pyrolysis oil) products as well as a coke consisting essentially of carbon, the so-called pyrolysis coke. In general, around 80% of the biomass is converted into gaseous products. It comes first at temperatures of significantly more than 100 ⁰ C to a Depoiymerisierung of polyoses or hemicelluloses and celluloses; this is accompanied by a splitting off of carbon dioxide and water of reaction. From about 340 ⁰ C alliphatische structures are broken up, and by debasing methane and other hydrocarbons are released. From about 400 ⁰ C there is a break-up of carbon-oxygen compounds, and it begins the decomposition of the large-molecular bitumen compounds formed in the meantime. At a further increase in temperature then further short-chain hydrocarbon compounds are formed. The composition of the products resulting from the pyrolytic decomposition (coke, oil, gas) essentially depends on the type and composition of the feedstocks, the heating rate and the achieved temperature level (slow versus rapid pyrolysis).

The products of the pyrolysis reactions form the educts of the reforming reactions in which hydrocarbons are separated from the hydrogen in two processes:

C _n H _m + n H ₂ O t; n CO + (n + m / 2) H ₂ CO + H ₂ OU CO ₂ + H ₂ (shift reaction)

The latter process serves to minimize the CO content in the product gas and the H ₂ -Antei! to maximize. At too low temperatures (<800 ^° C.) in the reformer reactor, the part of the reactor in which the allothermal gasification (pyrolysis) takes place, the degree of reforming of the pyrolysis residues (the pyrolysis coke) is low, resulting in a scfiuss these residues in the reformer reactor leads, which must then be discharged from the, in order to prevent overflow / clogging of the reformer reactor.

From EP 1 187 892 B1, a siphon-type construction is known for this purpose, with the aid of which the residues are discharged through a filter layer and via a siphon tube directly into a combustion chamber where they are thermally utilized by combustion. The bed of the filter layer and its "extent" in the siphon tube is a pressure seal or pressure-tight lock between the reformer reactor and the combustion chamber. By opening into the siphon nozzle nozzle, the material located therein is fluidized and from the siphon tube into the combustion chamber emptied.

The siphon-type construction disclosed in EP 1 187 892 B1 has the disadvantage that a simultaneous sealing and controlled emptying of the siphon tube is problematic and frequently leads to failures of the plant, which in turn has a safety risk in operating the plant as a consequence.

It is therefore an object of the present invention, starting from the device described in EP 1 187 892 B1, to provide a reactor for producing a product gas by allothermic gasification of carbonaceous starting materials, which avoids the abovementioned disadvantages.

This object is achieved by the Merkmaie of claim 1. The present invention is characterized in that a gas filter, which functionally corresponds to the filter layer described in EP 1 187 892 B1, and a pressure lock, the function of which is likewise taken over by the "filter layer" in EP 1 187 892 B1, are separate components are and that a derivative of the gas filter for solid particles is connected to the high pressure side of the pressure lock. In addition to the derivation for solid particles! the gas filter includes a discharge for product gas. In other words, in the gas filter, a separation of product gas and solid particles In takes place, wherein according to the invention via a pneumatic conveyor particulate gasification residues, in which raw gas is included, from the reformer reactor off and be supplied via the gas filter and the pressure lock the combustion chamber. The separation of the gas filter and the pressure lock offers the possibility of adapting and optimizing both independently of each other. Due to the features of claim 2, the risk of explosion of the otherwise very hot product gas can be reduced. Furthermore, this opens up freedom in the design of the subsequent gas filter, both constructive and in terms of materials, and the service life of the gas filter can be extended. The arrangement of the U-shaped pipe section and the riser pipe and thus the gas filter outside of the reformer reactor and outside the combustion chamber, so a total outside the reactor vessel, as defined in claim 3, allows a compact and, as the gas filter in the Design of the interior of the reactor vessel must not be considered constructive, simple construction and leads to a maintenance-related simplification of the entire system. In particular, in one embodiment according to claim 15, the height of the reactor container and thus in the promotion of the particulate gasification residues upwards such that this then takes place from the low pressure side of the gas filter in the combustion chamber gravity assisted reduced height difference to be overcome. The formation of the first part of the conveying path of the pneumatic conveyor as a downpipe, the promotion of particulate gasification residues also takes place within the reactor according to the invention, where the placement of a bulky conveyor is difficult or impossible to realize, advantageously gravity assisted.

The arrangement or orientation of the first downpipe according to claim 4 has in addition to the advantage of the above-described gravity-assisted promotion, which comes especially in a vertical arrangement to bear, the advantage that thereby the first downpipe with the implicitly defined in claim 1 device for the thermal coupling of the reformer Reactor with the combustion chamber at least collided.

The riser, in contrast to the U-shaped pipe piece, for example, to reduce frictional resistance, preferably straight, but at least formed longer over the latter, since it has to overcome the difference in height between the end of the U-shaped pipe section and gas filter. In this case, the comparatively long length of the riser allows a substantially equally long cooling section and thus a good cooling effect, while its straightness allows a constructive simplicity of the cooling device. Since both advantages in the u-shaped pipe section are not met to the same extent, an arrangement of the cooling device on the riser pipe according to claim 5 is advantageous.

The use of a steam generator as the cooling device according to claim 6, which can generate electrical energy in connection with a generator, for example, is advantageous both ecologically and economically. In particular, the electrical energy thus generated can be supplied to the system again.

As a result of the raw gas line defined in claim 7, part of the product gas produced during the allograft gasification in the reactor reformer is fed directly to the gas filter for the separation of particulate gasification residues contained therein. Another part is passed as gas entrapment into the particulate gasification residues discharged from the reactor reformer via the first downcomer to the gas filter. That is, according to the embodiment of claim 7 open two lines, the riser with its upper end and the crude gas line, in the gas filter, in which a separation or deposition of particulate gasification residues, which pass mainly through the riser into the gas filter, and the Raw gas, which passes mainly through the crude gas line into the gas filter takes place. By using the crude gas line, which directs the raw gas produced in the allothermal gasification directly to the gas filter, the raw gas and thus the product gas yield is increased, as in the other case, if the crude gas would not be present, the raw gas only together with the particulate gasification residues could be transported from the reformer reactor to the gas filter, which, however, can not remove the entire raw gas entrained in the particulate gasification residues.

In accordance with claim 8 define defined fluid supplies along the U-shaped pipe section and the riser for a safe "slipping" of the partikeiförmigen Gasification residues through these pipe sections. By parameters such as the amount of steam greased per unit time and the type of steam injection, which can be pulsating, for example, and thus except a fluidizing also has a "jolting" effect, the delivery resistance can be influenced and controlled.

The use of steam as a fluid according to claim 9 advantageously enables the at least partial use or process recycling of gases which are formed in the chemical processes taking place in the reactor vessel according to the invention, such as flue gases. Furthermore, the use of gases / steam has the advantage that a sudden evaporation, which occur at the given temperatures in the case of, for example, water and would at least make it difficult to controlled and uniform promotion, does not occur. Although the vapor already present in the gaseous state when it is introduced into the U-shaped tube and the riser also expands when it comes into contact with the very hot particulate residues, the expansion is far from being so rapid and causes bubbles to form For a relaxation of the "moving fixed bed" interpretable residues and by reducing the flow resistance also easier to overcome the height difference.A controllable, continuous and low-resistance funding is thus accompanied by an economical and safe operation of the entire system.

The use of a steam lance according to claim 10 allows an efficient and space-saving introduction of steam into the pneumatic conveyor, which can take place according to claim 11 via branching fluid feeds, for example, in regular or the weight of the combustion chamber bill bearing _« ie decreasing downward distances.

Due to the features of claim 12, it is possible to arrange the lock at a lower level than in a case in which the gas line defined there is not present and the riser must be performed to at least the same height as the gas filter. The product gas enclosed in the particulate gasification residues is removed here by the coarse separator and not by the gas filter, so that the gas filter is simpler and in particular more "fine-meshed". can be placed, which leads to a better quality of the final product gas produced.

Heatpipes for thermal coupling between the combustion chamber and the reformer reactor as defined in claim 13 have the advantage of allowing them to heat efficiently and quickly from a warmer place (here the combustion chamber) to a colder place The heat transfer in terms of heat quantity and speed can amount to 100-1000 times that of a geometrically identical component made of solid copper, and heat pipes can also be tuned by tuning, for example, their diameter, the type of their In particular, the working medium determines the temperature range in which the heat pipes can be used, and if the decision is made for capillary heat pipes in contrast to non-capillary heat pipes, the installation position has hardly any influence on their efficiency my formulated advantage of the vertical lead out of the first downpipe from the reformer reactor (claim 4) is concrete: The usual and advantageously straight rectified heat pipes can be arranged parallel to the first downpipe, preferably the combustion chamber and the reformer reactor, the are thermally coupled by the heat pipes, are arranged in a common reactor vessel, as defined in claim 14.

Due to the features of claims 16 and 17, a simplification of the design and thus the maintenance is obtained.

Due to the features of claim 18 both a thorough mixing in the case of a macroscopically homogeneous bed and also - in some situations desirable - due to the fluid behavior of the fluidized bed, to which the Archimedesprinzip can be applied, a vertical segregation in the case of an inhomogeneous bed achieved become. Furthermore, an excellent heat transfer both within the fluidized bed and between the fluidized bed and the device for thermal coupling between the combustion chamber and reformer reactor, for example, the defined in claim 13 heat pipes, achieved. The above and other objects, features and advantages of the present invention will become more apparent from the following detailed description made with reference to the accompanying drawings. In the drawings:

Fig. 1 is a schematic sectional view of a reactor according to a first embodiment of the present invention; Fig. 2 is a schematic sectional view of a reactor according to a second embodiment of the present invention;

Fig. 3 is a schematic sectional view of a reactor according to a third embodiment of the present invention;

Fig. 4 is a schematic sectional view of a reactor according to a fourth embodiment of the present invention; and

5 is a schematic sectional view of a reactor according to a fifth embodiment of the present invention.

1 shows a schematic sectional view of a reactor 10 for producing a product gas P by ailothermic gasification of carbonaceous feedstocks E according to a first embodiment of the present invention.

First embodiment

According to the first embodiment, the reactor 10 according to the invention for producing a product gas by ailothermic gasification of carbonaceous feedstocks comprises a reactor vessel 100, in which a combustion chamber 200 and a reformer reactor 300 are arranged, and a pipeline arranged outside the reactor 10. and feeder system 400. These components are described in detail below. The reactor vessel 100 includes a tube 102 having an annular cross section, a lower annular flange 104 and an upper annular flange 106. The reactor vessel 100 is below with a bottom 108 which is connected to the annular flange 104, and above with a lid 110, which is connected to the annular flange 106, sealed, being in the space between the ceiling! 110 and the annular flange 106 a Ringfiansch 304 of the reformer reactor 300 described below extends. The annular flanges 106, 304 and the lid 110 are releasably and tightly connected to each other, for example, by means of screws or the like mounted equidistantly along the circumference of the lid 110. The reactor vessel 100 has in its bottom 108 openings 112 through which at least a first pipe 114 and at least one second pipe 116, a primary air flow 142 and a secondary air flow 144 can be initiated in its lid 110 an opening 118 through which a Feed line 120 for supplying carbonaceous feedstocks E and auxiliaries in the reformer reactor 300 opens, and an opening 122, from which a crude gas line 402 for discharging part of the reformer reactor 300 resulting raw gas R is led out of the reformer reactor 300, and in its jacket an outlet opening 126 for discharging flue gas R arising in the combustion chamber 200 from the reactor vessel 100 and an inlet opening 128 through which particulate gasification residues can be introduced into the combustion chamber 200, as described below described in detail with the line and filter system 400 i st, up.

Concentric with the tube 102 in the reactor vessel 100, an insert 130 is also arranged annular cross-section which extends in the axial direction of the reactor vessel 100 from the bottom 108 to below the outlet opening 126 and has an outer diameter which is slightly smaller than the inner diameter of the tube 102 is such that a gap 132 with an annular cross-section is formed between the two. Parallel to the bottom 108 and tightly connected to the inside of the insert 130, a first separation bottom 134 and a second separation bottom 136 are arranged such that between the first separation bottom 134 and the second separation bottom 136 a first gas space 138 into which the first pipe 114 opens , and between the second separating tray 136 and the bottom 108, a second gas chamber 140 into which the second pipe 116 opens formed. The primary air flow 142 directed into the first gas space 138 through the first pipe 114 passes through holes (not shown) in the first separation bottom 134 from below into the combustion chamber 200. The secondary air flow 144 conducted through the second pipe 116 into the second gas space 140 passes through holes (not shown) in the peripheral wall of the second gas space 140 formed by the insert 130 into the gap 132 and through further holes (not shown) in the insert 130 as secondary air inflow 146 from the side into the combustion chamber 200 and the space between the combustion chambers 200 and the reformer reactor 300, primary and secondary air streams 142 and 144, 146 serve both as FluidisierungsmitteS for generating a fluidized bed in the combustion chamber 200 (see below) and as Oxidationsmitte! for the combustion reactions taking place there. The secondary air flow 144 also serves to thermally insulate the part of the circular cylindrical tube 102, which is located at the height of the combustion chamber 200 and is thus exposed to a high temperature. These and other details, such as the exact arrangement of the side holes, are described in detail in WO 2010/040787 A2 of the same Applicant. As shown in FIG. 1, the secondary air inflow 146 flowing laterally into the combustion chamber 200 undergoes a change in the flow direction upward through the primary air flow 142 flowing from below into the combustion chamber 200.

The combustion chamber 200 comprises a bed 202, which is converted by introducing the primary air flow 142 and the secondary air inflow 146 as fluidizing and oxidizing agent in a fluidized state, which corresponds to the operating state of the combustion chamber 200, and the bottom of the first separating floor 134 and is limited by a lower portion of the circular cylindrical insert 130, as shown in Fig. 1. The primary air flow 142 introduced into the first gas space 138 through the first pipe 114 passes through a plurality of holes or openings (not shown), which are preferably evenly distributed over the entire area of the first separation floor 134 and dimensioned such that the bed 202 passes through the first separation tray 134 is carried into the bed 202 or the fluidized bed created by the inflow. The bed 202 thus occupies a substantially circular cylindrical volume, which is energized by the jacket and the bottom of the fluidizing and oxidizing agent (primary and secondary air flow); she consists essentially of sand, which may be a catalyst is added, and fuels.

The reformer reactor 300 is according to this embodiment, as shown in Fig. 1, within the tube 102 and at a distance to and above the

Combustion chamber 200 arranged. The reformer reactor 300 comprises an outer blind tube 302 of annular cross section, on the open side (at the top in FIG. 1) of the flange 304 is formed, as described above, and an inner blind tube 306 with annular cross section, wherein the outer and inner sack tube 302, 306 are designed so that between them and limited by a limited in cross-section u-shaped gap space 308 and between the outer bag tube 306 and the tube 102 and by both a gap space 310 are formed. Overall, this results in an arrangement in which coincide according to the invention, the axes of symmetry of all elements with circular cross-section. As shown in FIG. 1, the side wall of the inner sack tube 306 does not extend to the lid 110, which, as explained below, allows overflow of the material in the inner sack tube 306 into the gap space 308 and generates a raw gas space 316 above the inner sack tube 306. The supply line 120 protrudes, as can be seen in Fig. 1, until just before the bottom 312 of the inner sack tube 306th

The combustor 200 and the reformer reactor 300 are coupled by heat pipes 204 that are capable of transporting heat from bottom to top in FIG. The heat pipes 204 each extend straight down almost to the first partition floor 134 and up almost to the level of the upper edge of the inner sack tube 306 and thereby penetrate the bottom 312 of the inner sack tube 306 and the bottom 314 of the outer outer tube 302th Die Passage surfaces of the heat pipes 204, of which only two can be seen in Fig. 1, by a plane perpendicular to the axis of symmetry are further arranged according to the embodiment uniformly distributed on a circle in this plane.

The line and filter system 400 includes a pneumatic conveyor 404, which in turn includes a gas filter 406, a pressure lock 408 having a high pressure side 408a connected to the gas filter 406, and a low pressure side 408b first downcomer 410, which is led out of the reactor vessel 100 substantially vertically downwards out of the reformer reactor 300, more specifically the slit space 308, out and through the combustor 200, the first and second separation trays 134, 136 and the bottom 108, a u-shaped pipe section 412 connected to the lower end of the first downpipe 410, a riser pipe 414 connected at one end to the other end of the u-shaped pipe section 412 and at its other end to the high pressure side 408a of the pressure lock 408 , and a second drop tube 416, which is connected at one end to the low-pressure side 408b of the pressure lock 408 and at the other end to the inlet opening 128 of the reactor container 100. In other words, the first drop tube 410, the U-shaped tube piece 412, and the riser tube 414 are integrally connected to an S-shaped tube that connects between the gap space 308 and the high pressure side 408a of the pressure lock 408. The pneumatic conveyor 404 further includes a steam lance 418 extending along the first downcomer 410 and over its entire length, and a fluidizing device 420 that extends throughout

Length along the U-shaped tube piece 412 and the riser 414 extends. In the line and filter system 400, the raw gas line 402 is further connected to the gas filter 406. As shown in Fig. 1, the arcuate upper end portion of the riser 414 is approximately level with the lid 110 of the reactor vessel 100. The height of a unit consisting of the spatially separated elements gas filter 406 and pressure lock 408, must be chosen so high that the slope of the second downpipe 416 is sufficient to promote the particulate gasification residues solely by gravity.

The operation of the reactor according to the invention is described below with reference to FIG. 1, in particular the current operation, and with regard to the start-up, reference is made to corresponding descriptions of fluidized bed reactors disclosed in further applications by the same applicant are. From the bed 202 of the combustor 200, a fluidized bed 142 and the secondary air inlet 146 of the secondary air stream 144 generates a fluidized bed formed essentially of the sand and the fuel. The heat generated by combustion of the fuel by means of the oxygen contained in the primary and secondary air 142, 144 is generated by the heat pipes 204 into another fluidized bed 318 formed in the reformer reactor 300, more specifically in the inner sack tube 306 is and is formed from the introduced via the feed tube 120 into the reformer reactor 300 carbonaceous feedstocks E and excipients, transported. As a result of the heat introduced in this way, the carbonaceous starting materials E are allothermally gasified, as described above. The particulate gasification residues, predominantly coke, produced in this process pass over the upper edge of the sack tube 306 and enter the gap 308 and thence into the first downcomer 410, the first section of the s-shaped tube carrying the reformer reactor 300 the high pressure side 408a of the pressure lock 408 connects. The particulate gasification residues are transported by the pneumatic conveyor 404 to the high pressure side 408a of the pressure lock 408, which is directly connected to the gas filter 406, wherein included in the particulate gasification residues raw gas by the gas filter 406 largely separated from the particulate gasification residues and as product gas P for further utilization is discharged to the outside. The particulate gasification residues which are largely freed from the enclosed tube gas are conveyed through the pressure lock 408, the second drop tube 416 and the inlet opening 128, which is arranged above the fluidized bed formed in the combustion chamber 200, into the reactor vessel 100 and are burned there. The raw gases produced during the allothermal gasification are also conducted via the crude gas line 402 directly to the gas filter 406, in which the raw gases, freed from the particulate gasification residues suspended therein, leave the reactor as product gas P.

Thus, in this embodiment, the gas filter 406 acts both as a fine filter for separating suspended particles from the raw gas R supplied through the pipe gas line 402 and as a coarse filter for separating raw gas R and particulate gasification residues fed via the riser 404. Second embodiment

2 shows a schematic sectional view of a reactor 10 for producing a product gas P by allothermic gasification of carbonaceous feedstocks E according to a second embodiment of the present invention. The reactor 10 according to the second embodiment differs from that of the first embodiment by a connecting line 422 between the lock 408 and the Rohgasieitung 402, resulting in a lower position and a limited function of the lock 408 results.

That is, according to the second embodiment, the lock 408 is now used for coarse separation, i. H. the separation of in the in the first downcomer 410, the u-shaped pipe section 412 and the riser 414 promoted particulate gasification residues from the enclosed therein raw gas R, which is supplied via the connecting line 422 of the crude gas line 402 and finally the gas filter 406. On the other hand, here the gas filter 406 only serves as a fine filter. The lock 408 occupies not only a lower position than the first embodiment, but is simultaneously moved closer to the reactor vessel 100, so that the second down pipe 416 between the low pressure side 408 b of the lock 408 and the reactor vessel 100 shortened and the Distance between the high pressure side 408 a and the gas filter 406 to a third down pipe 424, which serves to remove the particulate gasification residues from the raw gas R of the crude gas line 402 and the connecting line 422 from the gas filter 406, is extended. Third embodiment

3 shows a schematic sectional view of a reactor 10 for producing a product gas P by allothermic gasification of carbonaceous feedstocks E according to a third embodiment of the present invention. The reactor 10 according to the third embodiment differs from that of the first embodiment only in that the raw gas line 402 is omitted. The entire raw gas R which is produced during the gasification, together with the particulate gasification residues via the first downpipe 410 from the reformer Container 100 off and on the way described in connection with the first embodiment, the combustion chamber 200 supplied.

Fourth embodiment

4 shows a schematic sectional view of a reactor 10 for producing a product gas P by aothermal gasification of carbonaceous feedstocks E according to a fourth embodiment of the present invention. The reactor 10 according to the fourth embodiment differs from that of the third embodiment only in that the riser 404 is enclosed by a cooler 426. The cooling device 426 is designed according to the embodiment as a steam generator.

Fifth embodiment

5 shows a schematic sectional view of a reactor 10 for producing a product gas P by allothermic gasification of carbonaceous feedstocks E according to a fifth embodiment of the present invention. The reactor 10 according to the fifth embodiment differs constructively from that of the first embodiment in that the assembly of the first embodiment including the gas filter 406 and the pressure lock 408 is replaced by an assembly comprising a scrubber 428 including a cooling loop 430 for cooling the raw gas R and a pump 434. The scrubber 428 is subdivided into a first zone I, into which the raw gas line 402 and the riser 414 terminate, and in which the raw gas R is cooled and dusted, a second zone adjacent thereto II, which is connected to the pump 434 and in which a slurry, the tar condensate, water, dust and solvents, eg rapeseed methyl ester (RME), a by Umeste- tion of rapeseed oil with methanol-derived biodiesel fuel, contains, collected and pumped by the pump 434, and a product gas outlet side e third zone III, where water and tars condense. The pump 434 pumps the slurry via the second downcomer 416 through the inlet port 128 into the reactor vessel 100. Although the present invention has been disclosed in terms of the preferred embodiments in order to facilitate a better understanding thereof, it should be understood that the invention can be embodied in various ways without departing from the scope of the invention. Therefore, the invention should be understood to include all possible embodiments and embodiments to the illustrated embodiments which can be practiced without departing from the scope of the invention as set forth in the appended claims.

REFERENCE CHARACTERS

10 reactor

100 reactor tanks

102 circular cylindrical tube

104 lower ring flange of 102

106 upper ring flange of 102

108 floor of 102

110 lids of 102

112 openings

114 first pipe

116 second tube

118 opening in 110 for 120

120 supply line for E

122 opening in 110 for 402

126 outlet opening for R in 102

128 entrance opening in 102

130 use in 102

132 circular cylindrical gap

134 first separating tray

136 second separating tray 138 first gas space

140 second gas space

142 primary! uftstrom

144 secondary! uftstrom

146 secondary air infiltration

200 combustion chamber

202 bed

204 heat pipes

300 reformer reactor

302 outer sack tube

304 ring flange to 302

306 inner sack tube

308 u-shaped gap space

310 gap between 102 and 302

312 floor of 306

314 floor of 302

316 raw gas space

318 fluidized bed in 306

400 line and filter system

402 raw gas pipeline

404 pneumatic conveyor

406 gas filters

408 pressure lock

408a high pressure side of 408

408b low pressure side of 408

410 first downpipe

412 U-shaped piece of pipe

414 riser

416 second downpipe

418 steam lance

420 fluidizing device

422 connection line

424 third downpipe 426 cooling device

428 gas scrubbers

430 coolers

432 Dust washer 434 Pump

E starting materials

P product gas

R pipe gas

MII first to third zone of 428

Claims

claims

1 . Reactor (10) for producing a product gas (P) by aiothermal gasification of carbonaceous feedstocks (E), comprising:

a pressure-charged reformer reactor (300), in which a fluidized bed is formed, for the gasification of the carbonaceous feedstocks (E),

- A supply line (120) for supplying the carbonaceous feedstocks (E) and of auxiliaries for the gasification in the reformer reactor (300), - A combustion chamber (200) for generating the heat necessary for aiiotherme gasification, wherein the combustion chamber (200 ) is thermally coupled to the reformer reactor (300), and

- A pneumatic conveyor (404) for discharging particulate gasification residues and raw gas (R) from the reformer reactor (300) and for supplying the particulate gasification residues in the combustion chamber

(200), comprising a gas filter (406) for separating the particulate gasification residues from the raw gas (R) and a pressure lock (408) having a high pressure side (408a) and a low pressure side (408b), the gas filter (406) providing a drain for product gas (P) and a derivative for solid particles, characterized

- That gas filter (406) and pressure lock (408) are separate components and that the derivative of solid particles of the gas filter (406) with the high pressure side (408a) of the pressure lock (406) is connected.

2. Reactor (10) according to claim 1, characterized by a cooling device (426) for cooling the hot raw gas (R).

3. Reactor (10) according to one of the preceding claims, characterized in that in that the pneumatic conveying device (404) comprises a first drop tube (410) for discharging the particulate gasification residues from the reformer reactor (300),

in that the first downpipe (410) passes over a U-shaped pipe section (412) into a riser (414) having an upper end,

the U-shaped tube piece (412) and the riser pipe (414) are arranged outside the reformer reactor (300) and outside the combustion chamber (200),

- That the upper end of the riser pipe (414) with the gas filter (406) and the high pressure side (408a) of the pressure lock (408) is connected, and

in that a second drop tube (416) for feeding the particulate gasification residues into the combustion chamber (200) leaves from the low-pressure side (408b) of the pressure lock (408), 4. Reactor (10) according to claim 3, characterized in that the first drop tube (4) 410) proceeds substantially perpendicularly out of the reactor reformer (300).

5. Reactor (10) according to claim 3 or 4, characterized in that the cooling device (426) is arranged on the riser pipe (414).

6. Reactor (10) according to claim 5, characterized in that the cooling device (426) is a steam generator.

7. Reactor (10) according to any one of the preceding claims, characterized by a crude gas line (402) for supplying in the reformer reactor (300) resulting crude gas (R) to the gas filter (406).

8. Reactor (10) according to one of the preceding claims 2 to 7, characterized in that over the U-shaped pipe section (412) and the riser (414) distributed fluid feeds (420) are provided to support the pneumatic conveying. 9 reactor (10) according to claim 8, characterized in that the Fluidzufuhrun- gene (420) Dampfzufuhrungen

10. Reactor (10) according to one of the preceding claims 2 to 9, character- ized in that along the first downpipe (410) a fluid lance (418), in particular a steam lance, leads from the outside into the reformer reactor (300), to loosen the particulate gasification pressure levels in the reformer reactor (300) 1 1 reactor (10) according to claim 10, characterized in that branch off from the fluid lance (418) fluid feeds into the first downpipe

12 reactor (10) according to any one of the preceding claims 7 to 1 1, characterized in that the pressure lock (408) comprises a coarse separator for solids, which is connected via a gas line (422) with the crude gas line (402)

13. Reactor (10) according to one of the preceding claims, characterized in that the thermal coupling between the combustion chamber (200) and reformer reactor (300) by means of heat pipes (204) takes place

14 reactor (10) according to any one of claims 3 to 10, characterized in that the combustion chamber (200) and the reformer reactor (300) in a common reactor holder (100) are arranged and that the first downpipe (410) the combustion chamber chamber (200) and in the bottom area of the common reactor

Container (100) is guided to the outside

15 reactor (10) according to claim 14, characterized in that the reformer reactor (300) is arranged above the combustion chamber (200)

16. Reactor (10) according to claim 14 or 15, characterized in that the common reactor holder (100) and the reformer reactor (300) by a common cover! (1 10) are closed

17. Reactor (10) according to claim 16, characterized in that the reformer reactor (300) comprises a pot-shaped reactor housing (302) in which at a distance from the insides of the cup-shaped reactor vessel (302) an open-top cup-shaped insert ( 306) is arranged, in which the gasification reaction takes place, and that the first downpipe (410) opens into the bottom region of the pot-shaped reactor vessel (302),

18. Reactor according to one of the preceding claims, characterized in that in the combustion chamber, a fluidized bed is formed.