Abstract: The invention relates to a device (2) and a method for supplying combustion air and for recirculating exhaust gas for a burner (1) comprising a combustion chamber (10) and to a burner (1) comprising a device (2) for supplying combustion air and for recirculating exhaust gas. Multiple drive nozzles (21) distributed about a central axis (A) are used to supply combustion air to a mixing chamber (22) arranged downstream of the drive nozzles (21) by suctioning exhaust gases out of the combustion chamber (10); the combustion air exiting the drive nozzles (21) is mixed with exhaust gases in the mixing chamber (22) in order to form a combustion air/exhaust gas mixture, said exhaust gases flowing out of the combustion chamber (10) and being backflushed by means of the drive nozzles (21); and the combustion air/exhaust gas mixture is supplied to a reaction zone downstream of the mixing chamber (22).

Abstract: A process and apparatus for gasification of biomass. Biogenic residue may be supplied to a heating zone to dry the biomass and allow the volatile constituents to escape to generate a pyrolysis gas. The pyrolysis gas is supplied to an oxidation zone and substoichiometrically oxidized to generate a crude gas. The carbonaceous residue generated in the heating zone and the crude gas is partially gasified in a gasification zone. The gasification forms activated carbon and a hot process gas. The activated carbon and the hot process gas are conjointly cooled. The adsorption process during the conjoined cooling has the result that tar from the hot process gas is absorbed on the activated carbon in the cooling zone. A pure gas which is substantially tar-free is obtained. The tar-enriched activated carbon may be at least partly burned for heating the heating zone and/or the gasification zone.

Abstract: A method for heating a heating chamber to a temperature below the spontaneous ignition temperature of the fuel that is used, wherein fuel and air are reacted in flameless oxidation in a non-stoichiometric mixture ratio in a combustion chamber. The air ratio ? is at least lower than the stoichiometric ratio ?=1 such that the temperature in the combustion chamber does not exceed the temperature at which thermal nitrous oxide generation begins. Otherwise, ? is established such that the spontaneous ignition temperature of the fuel is exceeded. This results in two permissible air ratio ranges, between ?min and ?1 in sub-stoichiometric operation, and ?2 to ?max in superstoichiometric operation of the combustion chamber. The still-reactive gases released from the combustion chamber are made to react in the heating chamber, preferably by flameless oxidation. This avoids thermal nitrous oxide generation in the heating chamber.

Abstract: To heat a furnace chamber (16) indirectly using radiant tubes (11) to (14), heating energy is transferred through the radiant tube wall into the furnace chamber (16). During steady-state operation, the temperature in the radiant tube (11) to (14) and on its surface is higher than the furnace, depending on the specific heat output of the radiant tube (11) to (14). At a furnace temperature of 770° C. and a heat output of 50 kW/m2, the radiant tube has a temperature of 900° C. The radiant tube (11) to (14) can thus operate continuously with flameless oxidation at this output, even though the temperature in the furnace is only 100° C. However, if the radiant tube (11) to (14) has cooled to the furnace temperature of 770° C. during a break in burning, deflagration is avoided when the associated burner is ignited by initially operating said burner with a flame for a few seconds.

Abstract: A process and apparatus for gasification of biomass. Biogenic residue may be supplied to a heating zone to dry the biomass and allow the volatile constituents to escape to generate a pyrolysis gas. The pyrolysis gas is supplied to an oxidation zone and substoichiometrically oxidized there to generate a crude gas. The carbonaceous residue generated in the heating zone and the crude gas is partially gasified in a gasification zone. The gasification forms activated carbon and a hot process gas. The activated carbon and the hot process gas are conjointly cooled. The adsorption process during the conjoined cooling has the result that tar from the hot process gas is absorbed on the activated carbon in the cooling zone. A pure gas which is substantially tar-free is obtained. The tar-enriched activated carbon may be at least partly burned for heating the heating zone and/or the gasification zone.

Abstract: A recuperative burner (10) fires a furnace chamber (11) in a substoichiometric manner. The recuperative burner is arranged in a radiant tube (26) which is open towards and protrudes into the furnace chamber. Together with the recuperator (18) or a protrusion (21), the radiant tube (26) forms an exhaust gas channel (19) into which burn-out air is introduced by an air conducting device (23). The post-combustion which occurs in the exhaust gas channel (19) heats the radiant tube (26). The furnace chamber (11) is heated partly directly by fuel and air and partly indirectly by the radiant tube (26). An excessive level of CO emission is prevented by the post-combustion in the exhaust gas channel (19). By using the resulting heat from the radiant tube (26), excessively high exhaust gas temperatures are prevented and the thermal use of the fuel is optimized.

Abstract: To heat a furnace chamber (16) indirectly using radiant tubes (11) to (14), heating energy is transferred through the radiant tube wall into the furnace chamber (16). During steady-state operation, the temperature in the radiant tube (11) to (14) and on its surface is higher than the furnace, depending on the specific heat output of the radiant tube (11) to (14). At a furnace temperature of 770° C. and a heat output of 50 kW/m2, the radiant tube has a temperature of 900° C. The radiant tube (11) to (14) can thus operate continuously with flameless oxidation at this output, even though the temperature in the furnace is only 100° C. However, if the radiant tube (11) to (14) has cooled to the furnace temperature of 770° C. during a break in burning, deflagration is avoided when the associated burner is ignited by initially operating said burner with a flame for a few seconds.

Abstract: To improve the efficiency of recuperator burners, preferably to over 80%, a recuperator burner (10) is equipped with an auxiliary heat exchanger (26) which surrounds the recuperator (22), wherein both the recuperator and the auxiliary heat exchanger are preferably formed as purely counterdirectional-flow heat exchangers, wherein the auxiliary heat exchanger (26) has the air supplied to it on the side facing toward the furnace wall (11). The housing (15) around the auxiliary heat exchanger (26) can be cooled with cool air from the inside. In one configuration, the air is initially conducted to a flange cooler (45) to protect the region of the flange (16) against the exhaust-gas temperature. For example, the ceramic recuperator pipe (26) is resiliently pressed, and sealed off, against an outlet-side surface (35) of the auxiliary heat exchanger (26), which preferably has gap-like air ducts (39) formed in flattened pipes (40).

Abstract: A device for the flameless oxidation of fuel includes a flameless oxidation burner, a first conduit to convey a fluid fuel phase to a first outlet and a direct primary jet including the fluid fuel phase outwardly therefrom. A second conduit is provided to convey a jacketing gas to a second outlet. The second conduit is disposed surrounding the first conduit so as to direct a jacketing jet of the jacketing gas outwardly therefrom surrounding the primary jet.

Abstract: A radiant heat tube (5) comprises a tube body having a center section (6) and at least one recirculating section (7, 8) arranged next to the center section, said recirculating section forming a loop (9, 10) with said center section. A pivot joint bearing (23) is arranged on one end (12) of the radiant heat tube, while a sliding bearing (15) is arranged on the other end (11) of the radiant heat tube, said sliding bearing (15) being arranged opposite said pivot joint bearing (23). A burner (14) is disposed to heat the radiant heat tube (5).

Abstract: To improve the efficiency of recuperator burners, preferably to over 80%, a recuperator burner (10) is equipped with an auxiliary heat exchanger (26) which surrounds the recuperator (22), wherein both the recuperator and the auxiliary heat exchanger are preferably formed as purely counterdirectional-flow heat exchangers, wherein the auxiliary heat exchanger (26) has the air supplied to it on the side facing toward the furnace wall (11). The housing (15) around the auxiliary heat exchanger (26) can be cooled with cool air from the inside. In one configuration, the air is initially conducted to a flange cooler (45) to protect the region of the flange (16) against the exhaust-gas temperature. For example, the ceramic recuperator pipe (26) is resiliently pressed, and sealed off, against an outlet-side surface (35) of the auxiliary heat exchanger (26), which preferably has gap-like air ducts (39) formed in flattened pipes (40).

Abstract: Provision is made of a radiant heating pipe 10 which is designed to conduct hot gas through a central portion 14 in a preferred direction of flow SV, directed away from the burner 22, into at least one return portion 16, 18 and preferably at least partially back into the central portion 14, such that a recirculation flow through the radiant heating pipe 10 is produced overall. The smallest flow cross section DA for the gas in a zone 24, close to the burner, of the central portion 14 is smaller than the smallest flow cross section DE in a zone 26 remote from the burner. Preferably, the radiant heating pipe 10 according to the invention has a waist at the transition from a branching portion 13, close to the burner, to the central portion 14.

Abstract: In a burner and method for the operation of such a burner which is provided with first fuel and air supply means for FLOX® operation and second fuel and air supply means for operation with flame combustion, a control unit is provided for controlling fuel and air supply means in such a manner that, aided by flame combustion operation, the temperature required for FLOX® operation is rapidly achieved and FLOX® operation can be maintained at least in the region directly in front of the burner so as to provide for assisted FLOX® operation of the burner already before the conditions for pure FLOX® operation are established.

Abstract: In a highly efficient recuperator burner, which comprises at least one combustion chamber for warm-up operation and is otherwise set up for FLOX® operation, and a recuperator for preheating combustion air by means of thermal exhaust gas energy in a counter-current heat exchange mode via heat exchanger pipes, each heat exchanger pipe has, in a heat exchange section thereof, a flattened gap cross-section and, at its end facing a volume to be heated, a nozzle cross-section, which differs from the flattened gap cross-section of the heat exchanger pipe.

Abstract: In a high efficiency regenerator burner for heating spaces, the exhaust gas generated by the burner is provided which is conducted alternately through different regenerator cartridges and a partial stream of the exhaust gas is conducted under the control of an orifice plate through a bypass space in which the regenerator cartridges are disposed. A control structure is disposed in a burner head for controlling the exhaust gas bypass flow volume and also to control the main exhaust gas flow as well as the combustion air flow through the regenerator cartridges.

Abstract: A radiant heat tube (5) comprises a tube body having a center section (6) and at least one recirculating section (7, 8) arranged next to the center section, said recirculating section forming a loop (9, 10) with said center section. A pivot joint bearing (23) is arranged on one end (12) of the radiant heat tube, while a sliding bearing (15) is arranged on the other end (11) of the radiant heat tube, said sliding bearing (15) being arranged opposite said pivot joint bearing (23). A burner (14) is disposed to heat the radiant heat tube (5).

Abstract: In a high efficiency regenerator burner for heating spaces, the exhaust gas generated by the burner is provided which is conducted alternately through different regenerator cartridges and a partial stream of the exhaust gas is conducted under the control of an orifice plate through a bypass space in which the regenerator cartridges are disposed. A control structure is disposed in a burner head for controlling the exhaust gas bypass flow volume and also to control the main exhaust gas flow as well as the combustion air flow through the regenerator cartridges.

Abstract: In a highly efficient recuperator burner, which comprises at least one combustion chamber for warm-up operation and is otherwise set up for FLOX® operation, and a recuperator for preheating combustion air by means of thermal exhaust gas energy in a counter-current heat exchange mode via heat exchanger pipes, each heat exchanger pipe has, in a heat exchange section thereof, a flattened gap cross-section and, at its end facing a volume to be heated, a nozzle cross-section, which differs from the flattened gap cross-section of the heat exchanger pipe.

Abstract: In a burner and method for the operation of such a burner which is provided with first fuel and air supply means for FLOX® operation and second fuel and air supply means for operation with flame combustion, a control unit is provided for controlling fuel and air supply means in such a manner that, aided by flame combustion operation, the temperature required for FLOX® operation is rapidly achieved and FLOX® operation can be maintained at least in the region directly in front of the burner so as to provide for assisted FLOX® operation of the burner already before the conditions for pure FLOX® operation are established.