US20150111159A1 - Method for operating a multi-gas burner and a multi-gas burner - Google Patents

Method for operating a multi-gas burner and a multi-gas burner Download PDF

Info

Publication number
US20150111159A1
US20150111159A1 US14/400,494 US201214400494A US2015111159A1 US 20150111159 A1 US20150111159 A1 US 20150111159A1 US 201214400494 A US201214400494 A US 201214400494A US 2015111159 A1 US2015111159 A1 US 2015111159A1
Authority
US
United States
Prior art keywords
gas
calorific
nozzle
combustion
burner
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Abandoned
Application number
US14/400,494
Other languages
English (en)
Inventor
Holger Wulfert
André Baetz
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Loesche GmbH
Original Assignee
Loesche GmbH
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Loesche GmbH filed Critical Loesche GmbH
Assigned to LOESCHE GMBH reassignment LOESCHE GMBH ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: WULFERT, HOLGER, BAETZ, ANDRE
Publication of US20150111159A1 publication Critical patent/US20150111159A1/en
Abandoned legal-status Critical Current

Links

Images

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23D—BURNERS
    • F23D14/00—Burners for combustion of a gas, e.g. of a gas stored under pressure as a liquid
    • F23D14/20—Non-premix gas burners, i.e. in which gaseous fuel is mixed with combustion air on arrival at the combustion zone
    • F23D14/22—Non-premix gas burners, i.e. in which gaseous fuel is mixed with combustion air on arrival at the combustion zone with separate air and gas feed ducts, e.g. with ducts running parallel or crossing each other
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C9/00—Combustion apparatus characterised by arrangements for returning combustion products or flue gases to the combustion chamber

Definitions

  • the invention relates to a method for operating a multi-gas burner and to a multi-gas burner for operation with a low-calorific and a high-calorific combustion gas.
  • Generic multi-gas burners have in most cases a combustion chamber and at least one burner lance.
  • This burner lance is designed with a first, a second and a third nozzle.
  • a first, a second and a third feed chamber are provided which are each connected in terms of flow to a respective nozzle for feeding gases into the combustion chamber.
  • the nozzles of the at least one burner lance end on one side in the combustion chamber and on the other side in a respective feed chamber.
  • a burner muffle is provided in the combustion chamber in the region of the end of the nozzles.
  • a burner with a plurality of burner lances is described as a multiple lance burner.
  • Such gas burners are used in hot gas generators which are used to heat process gases, for example within the scope of smelting iron ores.
  • Hot process gases are required for a grinding-drying process of coal.
  • the ground and dried coal is further used in the smelting of iron ores.
  • combustion gases for hot gas generators generally low-calorific gases—also described as lean gases—are fed with an oxygen carrier for combustion, in particular air, through the nozzles into the combustion chamber, where they are then mixed with the oxygen carrier, ignited and combusted.
  • NO x Due to the higher calorific value of the high-calorific combustion gases they combust with a higher flame temperature in comparison with the low-calorific gases. It is hereby to be considered that, with effect from combustion temperatures above approximately 1300° C., NO x is formed through a thermal conversion of the N 2 of the oxygen carriers for the combustion, particularly with normal air. When using high-calorific combustion gases the combustion temperatures usually lie above this critical temperature range. The formation of NO x must, however, be extensively avoided in accordance with environmental protection legislation.
  • This object is achieved according to the invention through a method for operating a mul-ti-gas burner having the features of claim 1 and a multi-gas burner having the features of claim 10 .
  • a multi-gas burner having at least one burner lance with a first, a second and a third nozzle, having a first, a second and a third feed chamber, which are each connected in terms of flow to a respective nozzle, and having a combustion chamber, into which the at least one burner lance projects, is operated in such a way that in high-calorific operation air is introduced via the first nozzle and, simultaneously, O 2 -depleted gas is introduced via the second nozzle and a high-calorific combustion gas is introduced via the third nozzle into the combustion chamber, where they are reacted, in particular combusted, the air and the O 2 -depleted gas being used as oxygen providers or oxygen carriers for combustion.
  • the invention is based upon the recognition that in order to avoid the formation of NO x it is necessary to reduce the flame temperature in such a way that it lies below a range, in which the greatest amounts of NO x can be produced. This temperature range lies below approximately 1300° C.
  • ⁇ values in comparison with a low-calorific operation, that is to say a combustion of a low-calorific combustion gas.
  • the ⁇ value is also described as the combustion ratio or air ratio and defines the ratio of oxygen providers supplied for combustion, in particular air, to the minimum air quantity stoichiometrically required for the combustion of the combustion gas.
  • the ⁇ value increases.
  • the gases produced are cooled in case of complete combustion of the combustion gas. It can hereby be achieved that the whole combustion process takes place at a temperature lying below the critical temperature range for NO x production.
  • a further core idea of the invention can therefore be seen in not using exclusively normal air as an oxygen provider for combustion but instead mixing the oxygen provider for the combustion from normal air and O 2 -depleted gas.
  • the burner can hereby be operated with higher ⁇ values so that the previously described necessary reduction in the flame temperature is facilitated.
  • the process gas produced has a reduced oxygen content, in particular of less than 10%, so that the process gas can be used for example in coal grinding plants.
  • air is fed as an oxygen provider for combustion via the first nozzle and a low-calorific combustion gas is simultaneously fed via the second nozzle into the combustion chamber, where they are reacted, in particular combusted. It is hereby made possible to operate a multi-gas burner both with a low-calorific combustion gas and also with a high-calorific combustion gas and not to have to provide a separate burner for each of these operating modes.
  • This configuration is based upon the recognition that the nozzle which is used in low-calorific operation for the low-calorific combustion gas is not used in the high-calorific operation.
  • This nozzle can thus be used to admix O 2 -depleted gas to the air from the first nozzle in order to make the oxygen provider available for combustion.
  • the advantage of this solution in comparison with a provision of a further nozzle for the O 2 -depleted gas is that hereby the burner lances used for example only need to have three and not four nozzles. This reduces in particular the construction depth and construction dimensions of a multi-gas burner consisting of one or more such burner lances.
  • an outer nozzle is selected as the first nozzle, a central nozzle as the second nozzle and an inner nozzle of the burner lance as the third nozzle.
  • the combustion gas is blown in during low-calorific operation through a central nozzle so that the combustion gas, after being blown out of the nozzle, is surrounded by the air blown in and is efficiently mixed with it and can react with it.
  • the inner nozzle is used to blow in the high-calorific combustion gas.
  • the combustion of low-calorific gases is preferably carried out with ⁇ values in the range of from approximately 1.05 to approximately 1.2. Due to the low calorific values, between 2000 kJ/m N 3 and 4000 kJ/m N 3 , the combustion temperatures lie below 1300° C. As set out above, during high-calorific operation the multi-gas burner must be operated with higher ⁇ values in order to achieve the necessary reduction in the flame temperature. Depending upon the calorific value of the high-calorific gas used the ⁇ values lie in the range of from approximately 1.5 to approximately 2.0. When combusting coke gas for example the ⁇ value is preferably in the region of 1.6 whereby between 15% and 30% of the oxygen provider for the combustion is O 2 -depleted gas.
  • the ⁇ value in low-calorific operation and the ⁇ value as well as the admixing of O 2 -depleted gas in high-calorific operation are set in such a way that the hot process gases produced—also described as hot gases—have an O 2 content of less than 10%.
  • a lower target value of the O 2 content in the hot process gas can also be achieved through corresponding adaptation of the admixing of O 2 -depleted gas.
  • the quantity of the combustion gas, the ⁇ values and the composition of the oxygen provider for the combustion of air and O 2 -depleted gas can be set in such a way that the measured flame temperature does not exceed a value of approximately 1300° C.
  • the ⁇ value is hereby essentially determined by the quantity, that is to say the volume flow per time unit, of the combustion gas and the quantity of the oxygen provider for the combustion, since the proportions of the oxygen provider for the combustion which do not react with the combustion gas contribute to the cooling and reduction of the flame temperature.
  • a recirculated process gas e.g. from a grinding-drying process, in particular from a coal grinding plant
  • O 2 -depleted gas is used as O 2 -depleted gas.
  • a gas must be used as the process gas which has an oxygen content of less than 10%.
  • a so-called grinding-drying process is often hereby carried out, in which the coal to be ground or another starting substance is also dried in addition to being reduced in size.
  • hot process gases are necessary, but which must have an oxygen content of less than 10% due to explosion protection reasons.
  • process gases can be diverted from the grinding operation as O 2 -depleted gases for the operation of the multi-gas burner. If the hot process gases produced through the multi-gas burner are used for the grinding-drying operation, they are subsequently fed back into the grinding process so that no O 2 -depleted process gas is removed in total from the grinding process. It is of course also possible to use O 2 -depleted gas from other sources.
  • coking furnace gas is used as high-calorific gas and blast furnace gas as low-calorific gas.
  • Coal grinding plants with a hot gas generator which is constructed from a multi-gas burner are often used within the scope of ore preparation and processing, e.g. smelting processes.
  • Blast furnace gas is produced at the upper edge of the blast furnace, the blast furnace gas being available as a fa-vourable fuel for grinding-drying and the operation of the burner.
  • Any combustion gases such as for example synthesis gas, coke gas or natural gas can be used as high-calorific combustion gases.
  • the low-calorific gas can also be described as lean gas and the high-calorific gas as rich gas.
  • air within the scope of the invention this can be understood to mean in particular normal ambient air with an oxygen content of approximately 21%.
  • the gases added to the combustion gas within the scope of the combustion process are described within the scope of the invention as oxygen providers for the combustion.
  • the oxygen carrier or provider for the combustion can also be described as combustion air.
  • a low-calorific gas can be regarded as a gas with a combustion value or calorific value in the range of from approximately 2,000 to 4,000 kJ/m N 3 and a high-calorific gas as a gas with a combustion value or calorific value in the range of from approximately 10,000 to 40,000 kJ/m N 3 . It is not hereby entirely significant for the invention which combustion values the low-calorific and the high-calorific gas have but rather that the high-calorific gas has a higher combustion value than the low-calorific gas.
  • the invention further relates to a multi-gas burner for operation with a low-calorific and a high-calorific combustion gas.
  • a generic burner having a combustion chamber, at least one burner lance with a first, a second and a third nozzle, having a first, a second and a third feed chamber which are each connected in terms of flow to a respective nozzle in order to feed gases into the combustion chamber, wherein the nozzles terminate with one end in the combustion chamber and with another end in a respective feed chamber and the combustion chambers have a burner muffle in the region of the end of the nozzles, is further developed in that the first feed chamber is designed for feeding an oxygen provider for the combustion.
  • the second feed chamber is designed for feeding the low-calorific combustion gas and O 2 -depleted gas.
  • the third feed chamber is designed for feeding the high-calorific combustion gas.
  • a feed unit is provided for feeding the low-calorific combustion gas and the O 2 -depleted gas into the second feed chamber.
  • the feed unit is designed in such a way that either the low-calorific combustion gas or the O 2 -depleted gas is introduced into the second feed chamber in dependence upon the operating mode of the multi-gas burner.
  • a nozzle for the oxygen provider for the combustion and a second nozzle for the first combustion gas are used and in a second operation a third nozzle is used for the second combustion gas and furthermore the first nozzle for the oxygen provider for the combustion.
  • the multi-gas burner according to the invention has smaller construction dimensions, saves space and investment costs and can be more flexibly used. Material and outlay costs can also be saved as a construction of a burner lance with four nozzles requires more resources than the use of a burner lance with three nozzles.
  • a burner lance with three nozzles can hereby have an outer pipe, a central pipe and an intermediate pipe arranged between the outer pipe and the central pipe.
  • the pipes are respectively orientated coaxially relative to each other and arranged spaced apart from each other to form annular gaps or flow cross-sections.
  • the burner lance is thus constructed from three pipes coaxially inserted into each other, whereby each flow cross-section thereby produced is connected to a separate feed chamber.
  • the annular gap between the outer pipe and the intermediate pipe forms an outer nozzle
  • the annular gap between the intermediate pipe and the central pipe forms a central nozzle
  • the central pipe forms the inner nozzle.
  • the first nozzle is an outer nozzle
  • the second nozzle is a central nozzle
  • the third nozzle is an inner nozzle of a burner lance. It is further provided that the first nozzle is connected in terms of flow to the first feed chamber, the second nozzle to the second feed chamber and the third nozzle to the third feed chamber. It is hereby ensured that the air in both low-calorific and high-calorific operation is introduced through the outer nozzle.
  • the low-calorific combustion gas is introduced in low-calorific operation through the adjacent central nozzle and efficient mixing between the combustion gas and the air, which is the oxygen provider for the combustion, is thus facilitated.
  • the air is introduced through the outer nozzle and the O 2 -depleted gas through the central nozzle, whereby these can pre-mix with each other.
  • the high-calorific combustion gas is introduced through the inner nozzle.
  • control unit which is designed in low-calorific operation to introduce air into the first feed chamber, the low-calorific combustion gas into the second feed chamber and to block the supply to the third feed chamber.
  • the control unit is further designed in such a way that in high-calorific operation air is introduced into the first feed chamber, O 2 -depleted gas into the second feed chamber and the high-calorific combustion gas into the third feed chamber.
  • the cross-sectional area of the first nozzle relative to the second nozzle and to the third nozzle preferably has a ratio in the range of from 4.4-5.0:5.9-6.3:1, in particular 4.7:6.2:1.
  • the cross-sectional ratios can also be designed to deviate therefrom according to the gas used and depend essentially upon the ⁇ values used, the low-calorific and high-calorific combustion gas, the respective stoichiometric air requirement of the gases and/or the operating or blow-in pressure.
  • the design of the second nozzle can be significant for this purpose, as it is used for two different gases, on the one hand low-calorific combustion gas and in the other operating state O 2 -depleted gas.
  • a burner lance constitutes in the minimum case a complete multi-gas burner.
  • the desired burner output is achieved through the selection of the number of burner lances.
  • the individual burner lance is standard-ised to a certain output so that, in case of enlargement of the burner, no scale-up needs to be carried out. In this connection reference is made to “numbering-up”, i.e. modified criteria in relation to geometry, flow behaviour, etc. do not have to be considered in each burner configuration.
  • the invention further relates to a processing plant having a multi-gas burner according to the invention and a grinding plant for solid fuels, e.g. a coal grinding plant.
  • a processing plant having a multi-gas burner according to the invention and a grinding plant for solid fuels, e.g. a coal grinding plant.
  • a grinding plant for solid fuels e.g. a coal grinding plant.
  • It can in particular be a roller mill, wherein the coal grinding plant is provided as a means to be used as a source for O 2 -depleted gas.
  • the O 2 -depleted gas can be recirculated process gas from the grinding process, in particular a grinding/drying process.
  • any other thermal process i.e. use of a plurality of gases, low O 2 contents in the process gas and use thereof as recirculated gas, high regulating ratios, etc.
  • control unit which can also be designed as a control and regulating unit
  • the inflows of the different gases, the high-calorific combustion gas, the low-calorific combustion gas, the air and the O 2 -depleted gas can be correspondingly set in dependence upon the operating mode.
  • the control or regulation hereby takes place in such a way that in high-calorific operation the necessary calorific value is achieved with a flame temperature below 1300° C. and with a maximum oxygen content of in particular below 10% of the hot process gas.
  • the inflows in low-calorific operation are controlled by the control and regulating unit in such a way that an adequate calorific value is reached without reaching a flame temperature which is too high.
  • the low calorific value necessitates low combustion temperatures so that no significant O 2 problems arise in the process gas here.
  • the respective properties can be fixed in particular by setting the quantities of the gases used and the ratio of the gases to each other.
  • FIG. 1 shows a simplified structure of a multi-gas burner according to the invention.
  • FIG. 2 shows a process diagram of a coal grinding plant with a multi-gas burner according to the invention.
  • FIG. 1 shows a simplified structure of a multi-gas burner 1 according to the invention.
  • the multi-gas burner 1 shown here has two burner lances 10 which are respectively designed as three-lance burners or three-nozzle lances and have a first nozzle 11 , a second nozzle 12 and a third nozzle 13 .
  • the burner lances 10 end respectively in a combustion chamber 3 .
  • the multi-gas burner 1 further has a first feed chamber 21 , a second feed chamber 22 and a third feed chamber 23 .
  • the nozzles 11 , 12 , 13 of the burner lance 10 are formed by three pipes orientated coaxially relative to each other.
  • the first nozzle 11 ends in the first feed chamber 21 .
  • the second nozzle 12 ends in the second feed chamber 22 and the third nozzle 13 ends in the third feed chamber 23 .
  • the nozzles 11 , 12 , 13 or the end pipes can hereby be respectively fixed with flange-like connections to the inner wall of the respective feed chambers 21 , 22 , 23 .
  • a starting burner 17 is provided in the centre of the multi-gas burner 1 and is used to start the multi-gas burner 1 .
  • a feed 31 is provided for the first feed chamber 21 , a feed 32 for the second feed chamber 22 and a feed 33 for the third feed chamber 23 . Furthermore an ad-ditional fourth feed 34 is provided which also ends in the second feed chamber 22 .
  • the feeds 31 , 32 , 33 , 34 have valves which can be controlled via a control unit 36 .
  • the feed 31 is connected to an air source. It is hereby a matter of normal ambient air.
  • the feed line 32 is connected to a source for a low-calorific combustion gas. This can for example be blast furnace gas. Such low-calorific combustion gases are also called lean gases.
  • the feed line 33 is connected to a source for a high-calorific combustion gas which can also be described as a rich gas.
  • the feed line 34 is in turn connected to a source for O 2 -depleted gas. This can have in particular an O 2 content of less than 10%.
  • control unit 36 controls the valves of the feed 31 , 32 , 33 and 34 in such a way that air flows into the first feed chamber 21 via the feed line 31 and a low-calorific combustion gas flows into the second feed chamber 22 via the feed 32 .
  • the other two feed lines 33 and 34 are hereby closed.
  • the ratio of air which flows through the nozzle 11 into the combustion chamber 3 and the low-calorific gas which flows through the nozzle 12 into the combustion chamber 3 is adjusted so that the ⁇ value lies in the range of 1.1.
  • control unit 36 opens the valves of the feed lines 31 , 33 and 34 . Air hereby flows into the feed chamber 21 , O 2 -depleted gas into the feed chamber 22 and high-calorific gas into the feed chamber 23 . By means of the nozzles 11 , 12 , 13 these gases can flow into the combustion chamber 3 and react with each other there.
  • the control unit 36 hereby controls the inflow of air, of the O 2 -depleted gas and the high-calorific combustion gas in such a way that a ⁇ value in the region of 1.6 is set, whereby approximately 30% of the oxygen carrier for the combustion is O 2 -depleted gas.
  • swirl means can be provided in the region of the respective end of the nozzles in order to efficiently mix the out-flowing gases with each other.
  • the chamber 22 can be supplied both with the low-calorific combustion gas and with the O 2 -depleted gas.
  • the chamber 22 can be supplied both with the low-calorific combustion gas and with the O 2 -depleted gas.
  • the feed line 34 can be omitted.
  • FIG. 2 shows a process diagram of a coal grinding plant with a hot gas generator which uses a multi-gas burner 10 according to the invention.
  • a central element of the processing plant set out here is on the one hand the mill-classifier combination 52 , which can for example be a vertical roller mill with recirculating air operation, in particular a LOESCHE roller mill.
  • a hot gas generator 51 is provided which has a multi-gas burner 10 according to the invention.
  • the hot gas generator 51 serves to produce hot process gases or respectively to heat them, whereby these process gases are used within the scope of the grinding process in the mill-classifier combination 52 in order to dry the material to be ground, in this case raw coal, in addition to the grinding process.
  • a hot gas feed 54 is provided between the hot gas generator 51 and the mill-classifier combination 52 .
  • a coal grinding plant is to be regarded here merely as an example for a processing plant, in which a hot gas generator 51 is used. Instead of a mill-classifier combination 52 , other plant components can also be provided, in which generated hot process gas is used.
  • the raw coal to be ground is fed via a coal bunker 61 to the mill-classifier combination 52 .
  • the raw coal is ground to dust and dried with the aid of the hot gas which flows via the feed 54 into the mill-classifier combination 52 , is dried and transported in the direction of a filter 62 by means of air flow.
  • the carbon dust produced is separated and fed to a dust bunker 63 .
  • the carbon dust can then be removed from the dust bunker 63 and fed for its use, for example for PCI processes.
  • the process gas purified from the dust which process gas has also cooled in the meantime, is once again fed via a process gas recirculation means 56 to the hot gas generator 51 . It is heated here by the combustion energy and fed back via the hot gas feed 54 to the mill-classifier combination 52 .
  • the multi-gas burner 10 of the hot gas generator 51 has four different feeds.
  • Feed 71 serves for the feed of a low-calorific combustion gas, for example blast furnace gas, feed 72 for the feed of air, feed 73 for the feed of a high-calorific combustion gas, for example coke gas, and feed 74 for the feed of gas to the starting burner.
  • Natural gas can be used for example for this purpose.

Landscapes

  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Combustion Of Fluid Fuel (AREA)
  • Regulation And Control Of Combustion (AREA)
  • Pre-Mixing And Non-Premixing Gas Burner (AREA)
  • Air Supply (AREA)
  • Gas Burners (AREA)
US14/400,494 2012-06-05 2012-06-05 Method for operating a multi-gas burner and a multi-gas burner Abandoned US20150111159A1 (en)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/EP2012/002402 WO2013182214A1 (de) 2012-06-05 2012-06-05 Verfahren zum betrieb eines multigasbrenners sowie multigasbrenner

Publications (1)

Publication Number Publication Date
US20150111159A1 true US20150111159A1 (en) 2015-04-23

Family

ID=46458414

Family Applications (1)

Application Number Title Priority Date Filing Date
US14/400,494 Abandoned US20150111159A1 (en) 2012-06-05 2012-06-05 Method for operating a multi-gas burner and a multi-gas burner

Country Status (10)

Country Link
US (1) US20150111159A1 (xx)
EP (1) EP2834563B1 (xx)
JP (1) JP5890589B2 (xx)
KR (1) KR20150027054A (xx)
CN (1) CN104541102B (xx)
BR (1) BR112014029474A2 (xx)
CA (1) CA2871074C (xx)
IN (1) IN2014DN09007A (xx)
RU (1) RU2014145113A (xx)
WO (1) WO2013182214A1 (xx)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP3553378A1 (en) * 2018-04-13 2019-10-16 Linde Aktiengesellschaft Method and burner for combusting hydrogen sulphide
WO2024043841A1 (en) * 2022-08-22 2024-02-29 Turaş Gaz Armatürleri̇ San. Ve Ti̇c. A.Ş. Multi gas burner

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR102325814B1 (ko) * 2019-08-21 2021-11-11 씨에스케이(주) 스크러버용 버너

Citations (21)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE720507C (de) * 1936-10-14 1942-05-07 Krupp Fried Grusonwerk Ag Mahltrocknungsanlage
US4023921A (en) * 1975-11-24 1977-05-17 Electric Power Research Institute Oil burner for NOx emission control
US4097217A (en) * 1976-12-09 1978-06-27 The Keller Corporation Method for converting combustor from hydrocarbonaceous fuel to carbonaceous fuel
US4169700A (en) * 1976-09-10 1979-10-02 Nippon Steel Corporation Burner for a regenerative hot blast stove
US4270466A (en) * 1978-10-21 1981-06-02 Klockner-Humboltd-Deutz AG Method and apparatus for rendering an ignitable fuel-oxygen mixture inert
JPH08127811A (ja) * 1994-10-28 1996-05-21 Sumitomo Metal Ind Ltd 熱風炉の燃焼制御方法
US5743723A (en) * 1995-09-15 1998-04-28 American Air Liquide, Inc. Oxy-fuel burner having coaxial fuel and oxidant outlets
NL1005439C2 (nl) * 1997-03-05 1998-09-08 Hoogovens Staal Bv Werkwijze voor het bedrijven van een gasturbine.
US6019595A (en) * 1996-07-05 2000-02-01 Loesche Gmbh Burner
US6126438A (en) * 1999-06-23 2000-10-03 American Air Liquide Preheated fuel and oxidant combustion burner
US20030108839A1 (en) * 1999-12-23 2003-06-12 Watson Richard William Partial oxidation of hydrogen sulphide
US20060275724A1 (en) * 2005-06-02 2006-12-07 Joshi Mahendra L Dynamic burner reconfiguration and combustion system for process heaters and boilers
US20070207419A1 (en) * 2005-12-28 2007-09-06 Jupiter Oxygen Corporation Oxy-fuel combustion with integrated pollution control
US20080261162A1 (en) * 2002-08-14 2008-10-23 Roger Lanary Burner and method of burning gas in a furnace
US20090111064A1 (en) * 2007-10-30 2009-04-30 Air Products And Chemicals, Inc. Burner System And Method Of Operating A Burner For Reduced NOx Emissions
US20100081098A1 (en) * 2008-09-26 2010-04-01 Air Products And Chemicals, Inc. Combustion System with Precombustor for Recycled Flue Gas
US20100183990A1 (en) * 2009-01-16 2010-07-22 Air Products And Chemicals, Inc. Multi-Mode Combustion Device and Method for Using the Device
US20100199722A1 (en) * 2007-06-08 2010-08-12 Saint-Gobain Emballage Dilute combustion
US20110109021A1 (en) * 2009-11-06 2011-05-12 Cain Bruce E Apparatus and Methods for Achieving Low NOx in a Grate-Kiln Pelletizing Furnace
US20130048767A1 (en) * 2010-04-23 2013-02-28 Loesche Gmbh Method for comminution of mill feed
US20130269576A1 (en) * 2010-11-18 2013-10-17 Linde Aktiengesellschaft Burner with adjustable flue gas recirculation

Family Cites Families (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS5664210A (en) * 1979-10-26 1981-06-01 Chugai Ro Kogyo Kaisha Ltd Multi gas burner
DE2948048C2 (de) * 1979-11-29 1981-10-08 Aichelin GmbH, 7015 Korntal Industriebrenner
CN2110139U (zh) * 1991-09-17 1992-07-15 石家庄市焊割炬厂 三气火焰加热器喷嘴
DE4208951C2 (de) 1992-03-19 1996-01-18 Loesche Gmbh Heißgaserzeuger
CN1224490A (zh) * 1996-07-05 1999-07-28 勒舍有限公司 燃烧器
US6241510B1 (en) * 2000-02-02 2001-06-05 Praxair Technology, Inc. System for providing proximate turbulent and coherent gas jets
CN2539062Y (zh) * 2002-05-22 2003-03-05 邯郸钢铁股份有限公司 蜂窝体蓄热式烧嘴
US8408197B2 (en) * 2008-10-13 2013-04-02 Corning Incorporated Submergible combustion burner
CN101382387B (zh) * 2008-10-22 2011-11-30 中国恩菲工程技术有限公司 有色金属熔炼侧吹炉喷枪

Patent Citations (23)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE720507C (de) * 1936-10-14 1942-05-07 Krupp Fried Grusonwerk Ag Mahltrocknungsanlage
US4023921A (en) * 1975-11-24 1977-05-17 Electric Power Research Institute Oil burner for NOx emission control
US4169700A (en) * 1976-09-10 1979-10-02 Nippon Steel Corporation Burner for a regenerative hot blast stove
US4097217A (en) * 1976-12-09 1978-06-27 The Keller Corporation Method for converting combustor from hydrocarbonaceous fuel to carbonaceous fuel
US4270466A (en) * 1978-10-21 1981-06-02 Klockner-Humboltd-Deutz AG Method and apparatus for rendering an ignitable fuel-oxygen mixture inert
JPH08127811A (ja) * 1994-10-28 1996-05-21 Sumitomo Metal Ind Ltd 熱風炉の燃焼制御方法
US5743723A (en) * 1995-09-15 1998-04-28 American Air Liquide, Inc. Oxy-fuel burner having coaxial fuel and oxidant outlets
US6019595A (en) * 1996-07-05 2000-02-01 Loesche Gmbh Burner
NL1005439C2 (nl) * 1997-03-05 1998-09-08 Hoogovens Staal Bv Werkwijze voor het bedrijven van een gasturbine.
US6126438A (en) * 1999-06-23 2000-10-03 American Air Liquide Preheated fuel and oxidant combustion burner
US20030108839A1 (en) * 1999-12-23 2003-06-12 Watson Richard William Partial oxidation of hydrogen sulphide
US20030133850A1 (en) * 1999-12-23 2003-07-17 Watson Richard William Partial oxidation of hydrogen sulphide containing gas
US20080261162A1 (en) * 2002-08-14 2008-10-23 Roger Lanary Burner and method of burning gas in a furnace
US20060275724A1 (en) * 2005-06-02 2006-12-07 Joshi Mahendra L Dynamic burner reconfiguration and combustion system for process heaters and boilers
US20070207419A1 (en) * 2005-12-28 2007-09-06 Jupiter Oxygen Corporation Oxy-fuel combustion with integrated pollution control
US20100199722A1 (en) * 2007-06-08 2010-08-12 Saint-Gobain Emballage Dilute combustion
US20090111064A1 (en) * 2007-10-30 2009-04-30 Air Products And Chemicals, Inc. Burner System And Method Of Operating A Burner For Reduced NOx Emissions
US20100081098A1 (en) * 2008-09-26 2010-04-01 Air Products And Chemicals, Inc. Combustion System with Precombustor for Recycled Flue Gas
US9243799B2 (en) * 2008-09-26 2016-01-26 Air Products And Chemicals, Inc. Combustion system with precombustor for recycled flue gas
US20100183990A1 (en) * 2009-01-16 2010-07-22 Air Products And Chemicals, Inc. Multi-Mode Combustion Device and Method for Using the Device
US20110109021A1 (en) * 2009-11-06 2011-05-12 Cain Bruce E Apparatus and Methods for Achieving Low NOx in a Grate-Kiln Pelletizing Furnace
US20130048767A1 (en) * 2010-04-23 2013-02-28 Loesche Gmbh Method for comminution of mill feed
US20130269576A1 (en) * 2010-11-18 2013-10-17 Linde Aktiengesellschaft Burner with adjustable flue gas recirculation

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP3553378A1 (en) * 2018-04-13 2019-10-16 Linde Aktiengesellschaft Method and burner for combusting hydrogen sulphide
WO2024043841A1 (en) * 2022-08-22 2024-02-29 Turaş Gaz Armatürleri̇ San. Ve Ti̇c. A.Ş. Multi gas burner

Also Published As

Publication number Publication date
RU2014145113A (ru) 2016-07-27
EP2834563B1 (de) 2016-03-02
CN104541102B (zh) 2017-03-15
CA2871074A1 (en) 2013-12-12
KR20150027054A (ko) 2015-03-11
EP2834563A1 (de) 2015-02-11
CN104541102A (zh) 2015-04-22
CA2871074C (en) 2019-02-26
WO2013182214A1 (de) 2013-12-12
JP2015522785A (ja) 2015-08-06
IN2014DN09007A (xx) 2015-05-22
BR112014029474A2 (pt) 2017-06-27
JP5890589B2 (ja) 2016-03-22

Similar Documents

Publication Publication Date Title
EP2623861A1 (en) Combustion system and method for operating same
AU2012294314B2 (en) Low NOx Fuel injection for an indurating furnace
RU2533269C2 (ru) Модуль горелки для сталелитейных установок
JP2016522133A (ja) セメント製造プラントの運転方法
CA2871074C (en) Method for operating a multi-gas burner and a multi-gas burner
EP2751484B1 (en) Combustion apparatus with indirect firing system
KR20120094949A (ko) 고로 열풍로 가열 방법
JP6016815B2 (ja) 熱風炉を加熱するための装置と方法
JP2005272297A (ja) セメントクリンカの製造方法
US5141726A (en) Process for reducng Nox emissions from combustion devices
CN109340789A (zh) 炭黑尾气低氮稳燃工艺及炭黑尾气低氮稳燃系统
CN210399972U (zh) 一种水泥分解炉煤粉高效气化低氮燃烧技术装置
US7682447B1 (en) Cement clinker production with reduced emissions
US20100244337A1 (en) NOx Suppression Techniques for an Indurating Furnace
TW201508225A (zh) 用於操作多氣體燃燒器的方法與多氣體燃燒器
JP2013217579A (ja) 石炭とバイオマスの混焼装置及びこれを備えたボイラ
dos Santos Mateus et al. Modern Kiln Burner Technology in the Current Energy Climate: Pushing the Limits of Alternative Fuel Substitution
EP2742285B1 (en) Low no× fuel injection for an indurating furnace
CN115751359A (zh) 一种阶梯燃烧烟气循环系统
JP2016089134A (ja) ガス化炉及びガス化炉への燃料投入方法
JPH06265105A (ja) 微粉固体燃料燃焼装置

Legal Events

Date Code Title Description
AS Assignment

Owner name: LOESCHE GMBH, GERMANY

Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:WULFERT, HOLGER;BAETZ, ANDRE;SIGNING DATES FROM 20141202 TO 20141205;REEL/FRAME:034512/0641

STCB Information on status: application discontinuation

Free format text: ABANDONED -- FAILURE TO RESPOND TO AN OFFICE ACTION