EP0210205B1 - Vorrichtung zur verbrennung von flüssigen und gasförmigen brennstoffen mit stickoxidfreien abgasen - Google Patents

Vorrichtung zur verbrennung von flüssigen und gasförmigen brennstoffen mit stickoxidfreien abgasen Download PDF

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Publication number
EP0210205B1
EP0210205B1 EP86900771A EP86900771A EP0210205B1 EP 0210205 B1 EP0210205 B1 EP 0210205B1 EP 86900771 A EP86900771 A EP 86900771A EP 86900771 A EP86900771 A EP 86900771A EP 0210205 B1 EP0210205 B1 EP 0210205B1
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EP
European Patent Office
Prior art keywords
combustion
gas
chamber
unit according
cooled
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.)
Expired - Lifetime
Application number
EP86900771A
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German (de)
English (en)
French (fr)
Other versions
EP0210205A1 (de
Inventor
Christian Dr.-Ing. Koch
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.)
KAT-TEC GESELLSCHAFT fur KATALYSATORTECHNIK MBH
Original Assignee
KAT-TEC KATALYSATORENTECH GmbH
Kat-Tec Gesellschaft fur Katalysatortechnik Mbh
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.)
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Publication date
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Priority to AT86900771T priority Critical patent/ATE58219T1/de
Publication of EP0210205A1 publication Critical patent/EP0210205A1/de
Application granted granted Critical
Publication of EP0210205B1 publication Critical patent/EP0210205B1/de
Anticipated expiration legal-status Critical
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Classifications

    • 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 
    • F23C13/00—Apparatus in which combustion takes place in the presence of catalytic material
    • 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 
    • F23C6/00—Combustion apparatus characterised by the combination of two or more combustion chambers or combustion zones, e.g. for staged combustion
    • F23C6/04—Combustion apparatus characterised by the combination of two or more combustion chambers or combustion zones, e.g. for staged combustion in series connection
    • F23C6/045—Combustion apparatus characterised by the combination of two or more combustion chambers or combustion zones, e.g. for staged combustion in series connection with staged combustion in a single enclosure
    • F23C6/047—Combustion apparatus characterised by the combination of two or more combustion chambers or combustion zones, e.g. for staged combustion in series connection with staged combustion in a single enclosure with fuel supply in stages
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F24—HEATING; RANGES; VENTILATING
    • F24D—DOMESTIC- OR SPACE-HEATING SYSTEMS, e.g. CENTRAL HEATING SYSTEMS; DOMESTIC HOT-WATER SUPPLY SYSTEMS; ELEMENTS OR COMPONENTS THEREFOR
    • F24D19/00—Details
    • F24D19/008—Details related to central heating radiators
    • F24D19/0085—Fresh air entries for air entering the room to be heated by the radiator

Definitions

  • the invention relates to a combustion unit for liquid and / or gaseous fuels with air in a heat generator.
  • a device for generating fission gas in which fuel from hydrocarbon and air are mixed in a "rich" mixture ratio in a combustion chamber. After their ignition and combustion, the resulting combustion gases leave the combustion chamber, heat a catalytic reaction chamber via a heat exchanger and - before they enter it - are again mixed with fuel of the above type. This prevents the second supply line of fuel from coming into direct contact with the flames in the combustion chamber. This is to achieve an endothermic reaction with little air or little oxygen in the downstream catalytic reaction chamber, so that heat dissipation is avoided.
  • the problem of the combustion of fuel gases without nitrogen oxides has not been addressed.
  • the invention proposes a combustion unit of the type mentioned at the outset, which has the following: a combustion chamber, into which a fuel / air mixture is fed via a first line; an ignition device for the fuel / air mixture to form a hot combustion gas; a cooled outer wall belonging to the combustion chamber for cooling the combustion gas; a mixing space which is formed within the combustion chamber for mixing the cooled combustion gases with additional fuel, the additional fuel being admixed via a second line; a catalytic reaction chamber downstream of the combustion chamber for reaction with the cooled combustion gases which are already mixed with the additional fuel; and a heat exchanger downstream of the catalytic reaction chamber.
  • the combustion unit can be provided with a line leading from the heat exchanger, which line is connected to the first and second line of a downstream combustion unit, preferably of the type according to the invention.
  • the reaction of the conversion of the fuel with the air is achieved at all points, so that the heat release by the combustion reactions and subsequent flue gas cooling can take place in a temperature range below 1300 ° C. or under a reducing atmosphere, or nitrogen oxides formed in a reducing atmosphere under catalytic action can be reduced.
  • Only about half of the gaseous fuel, in the range between 30 and 70%, is almost completely burned with the total air of the first stage in a preliminary stage in a cooled ring chamber.
  • the hot flue gases only cool down to temperatures of 1200 to 1600 ° C in the annular chamber, which only has 1-2% of the total heat exchange surface.
  • the conversion in the 1st stage takes place in that a partial stream of the gasification gas formed is returned to the ring chamber of the 1st stage and there completely burns with the partial stream of air.
  • the amount of liquid fuel added is added to the hot combustion gas at the top of the 1st stage.
  • the mixture converts to a fuel gas in the 1st stage catalyst.
  • the uppermost ceramic or metal plate of the catalyst unit at the point where the liquid jet hits meets.
  • This plate has a hole that is so small that only about half of the oil reaches the next plate directly. The scarce half of the injected oil is reflected and burned in the flame above the plate.
  • the resulting flue gases cool down partly with radiation and convection with the surrounding water-cooled surfaces, mix with the unburned oil to form a reactive mixture and are converted into fuel gas in the subsequent catalyst block.
  • the subsequent heat exchanger ensures that the heat content in the exhaust gas is almost completely given off to the heating medium in the pipes, for example process water or water from the heating circuit.
  • the almost complete heat dissipation is favored by the fact that combustion of the gas in the catalytic converter does not result in a flame volume and no soot-containing by-products which impair the heat transfer to the pipes.
  • the device according to the invention consists of the mixing heads of the two stages closed off with perforated plates with the gas inlets in the upper part of the head and the gas outlets through the perforated plates, from the cooled annular chambers with the mixture inlets and ignition devices with the catalyst located in the center and the subsequent heat exchangers.
  • the device contains the gas transfers from the 1st stage with an inlet into the ring chamber of the 2nd stage and an introduction into the mixing head.
  • the first line for the entry of the gas-air mixture of the 1st stage is designated, which admits the fuel gas stream mixed with the combustion air of the 1st stage into the annular combustion chamber 103 of the 1st stage.
  • This fuel gas-air flow is ignited by the ignition device, for example a spark plug 102.
  • the hot burned gas sweeps along the medium-cooled outer wall 125 on the way up through the combustion chamber 103 and is thereby cooled.
  • the partially cooled exhaust gas reaches the head of the combustion chamber 103, where the remaining amount of fuel gas is mixed with the hot flue gas.
  • the hot flue gas sucks in the remaining amount of fuel gas in this gap, which is introduced into the gas chamber 108 from above through the perforated plate 106.
  • the mixing of the components is improved by the inlet opening 109 and the chamber-like mixing space 110 located in front of the catalyst, so that the hot mixture has a homogeneous concentration distribution when introduced into the catalyst 111 of the catalytic reaction chamber 107.
  • the catalyst 111 can consist of a catalyst honeycomb that prevents the gases from mixing in the catalyst.
  • the catalyst 111 is clamped by an insulation mat 112 in the housing 113 and thermally insulated, so that the active substance of the catalyst 111 remains protected by the higher temperatures in the combustion chamber 103 surrounding the catalyst.
  • the heat exchanger 114 is arranged, which cools the resulting cracked gas to a temperature above the dew point temperature.
  • the cracked gas discharged from the heat exchanger 114 into the line 115 passes through the line 116 together with the combustion air of the second stage into the channel-like and annular combustion chamber 117 of the second stage.
  • the ignition device 118 which ignites the mixture of the combustion chamber 117, is also located there.
  • the combustion of the amount of cracked gas in the annular chamber is highly stoichiometric, i.e. the amount of air is sufficient to completely burn the gas.
  • the gas chamber 119 At the upper end of the annular chamber is the gas chamber 119, which catalyzes the perforated plate 120 and the upper cover plate of the other table reaction chamber 121 forms the mixing chamber of the flue gas of the combustion chamber and the remaining amount of fission gas. This subset of the cracked gas is introduced into the gas chamber 119 through the line 122.
  • the mixture of the flue gas with excess air and the cracked gas enables the gas 123 to be converted into a slightly overstoichiometric flue gas from which the heat can be obtained quite effectively.
  • Fig. 2 shows a further structure of the cracked gas generating part according to the invention.
  • the base body which contains the device for the ignition device 204 and for the injection nozzle 202, which injects the fuel discontinuously and in a controlled manner, is designated by 201.
  • the flame chamber of the combustion chamber 211 is designated by 203, where the flame, which is cooled by the surrounding water-cooled outer walls 205, is formed by the reflection of part of the oil, the mixing with the gasification air, and ignition by the ignition device 204.
  • a part of the gasification air is led directly into the vicinity of the ignition device 204 through a small bore 206 which is provided with an air filter 207.
  • the cooling of the base body 201 takes place in such a way that the required gasification air is sucked through the inlet opening 208 of the cover hood 209, in order to then sweep past the surface of the base body 201 and to pass through the outlet 210 into the foot of the combustion chamber 211 below the flame arrester 212.
  • the hot flue gases arising in the flame chamber 203 mix with the unburned oil, which was not reflected by the storage plate 213 with the bore 214.
  • the mixture enters the catalyst 215, which consists of one or more catalyst blocks.
  • the catalyst 215 consists of one or more catalyst blocks.
  • the mixture of hot flue gas and oil vapor converts to a cracked gas consisting essentially of CH4, CO, H2 and the exhaust gas components.
  • the hot cracked gases are cooled in a subsequent heat exchanger (not shown in FIG. 2) and mixed with air in the second stage in accordance with the content of the older national DE application P 35 03 413.0 converted to flue gas.
  • FIG. 3 shows the construction of the combustion part according to the invention.
  • 320 with the base plate is designated, through the inlet 321, a portion of the cracked gas can flow into the combustion chamber 322.
  • the combustion air flows through the throttle device 323 to the outlet opening 324 and thereby cools the base plate 320.
  • the air preheated in this way mixes at 325 with the remaining cracked gas.
  • This mixture is ignited with the ignition device 326.
  • the flame cools down on the surrounding water-cooled wall surface 327.
  • the exhaust gases mix with the cracked gas from 321.
  • the catalyst system 328 which can consist of one or more catalyst blocks, the oxidation takes place with the remaining cracked gas products to give exhaust gas.
  • Fig. 4 shows the structure of a heat exchanger element.
  • the split or exhaust gas flows through the pipes 31 fastened in the base plate 30 and heats the cooling water on the shell side, which enters at 32 and exits again at 33. Due to the round outer cylinder of the heat exchanger 34, increased water pressure with thin walls is possible.
  • the fission gas generation part is symbolized by 40 and the combustion part by 41.
  • 42 denotes the cracked gas heat exchanger in the form as shown in FIG. 4.
  • 43 denotes the heat exchanger system, consisting of one or more heat exchanger elements of the same type, as they were shown in Fig. 4.
  • the heating oil for heat and fission gas is injected at 44.
  • the air for the partial combustion enters the cover at 45, leaves it at 46 and is then passed below the flame arrester at 47 into the annular space.
  • the cracked gas leaves the cracked gas generating part 40 and is cooled in the heat exchanger 42.
  • a part of the cracked gas leaves the idle train 50 at 49 in order to be guided into the head of the combustion part 41 via a control member 51 at 53.
  • the remaining part of the cracked gas is branched off, at 59 mixed with the air; which enters the cover at 60 via the throttle element 61 and exits again at 62.
  • the hot exhaust gases leave the combustion part 41 at 54, are cooled in the heat exchanger system 43 and leave the device according to the invention at 55.
  • the blower 56 generates the resistance-related negative pressure in the device and thus sucks all gases through the device and sends them into the chimney 57.
  • the cold water enters the heat exchanger system 43 at 63, passes through the pipe connection 64 into the fission gas heat exchanger 42, which it leaves again at 65.
  • the water enters the foot of the annular gap of the cracked gas generating part 40 and is conducted at the head thereof via the pipe connection 67 into the annular gap of the combustion part 41. Warmed to its usage temperature, the warm water leaves the device according to the invention at 68 in order to be forwarded to the individual consumers via line 69.
  • the first exemplary embodiment (FIG. 1) describes the temperature and volume flow curve of a nitrogen oxide-free combustion of natural gas with a thermal output of 100 kW.
  • the volume flow data refer to the standard state (0 ° C, 760 Torr).
  • a possibly inserted spiral made of heat-resistant material forces the exhaust gas jet to wind around 3 times on the way into the annular chamber head around the catalyst 111.
  • the exhaust gases sweep along the water-cooled outer wall 125 and cool down to about 1600 ° C.
  • the exhaust gases When entering the mixing gap 105, the exhaust gases accelerate and generate a negative pressure, which causes a gas quantity of 0.001393 m 3 / s to be drawn in from the gas chamber 108 via the perforated plate 106.
  • the gas which is now homogeneously mixed, passes through the inlet opening 109 and the mixing space 110 through the catalyst 111, where it reacts to 0.01884 m 3 / s of cracked gas in endothermic processes.
  • the gasification gas Before entering the first stage heat exchanger 114, the gasification gas has a temperature of 886 ° C. and a temperature of approximately 130 ° C. at the outlet.
  • the cracked gas leaves the 1st combustion stage via line 115.
  • the gas circulates with the aid of a heat-resistant spiral about 3 times around the catalyst 123 and cools down to about 1060 ° C. on the water-cooled outer wall 126.
  • the remaining amount of cracked gas of 0.00471 m 3 / s is fed to the flue gas via line 122 of gas chamber 119 and perforated plate 120, mixed homogeneously via the inflow opening and the mixing chamber and fed to the catalyst.
  • the flue gas / cracked gas mixture is converted into 0.02932 m 3 / s flue gas in exothermic processes.
  • the flue gas Before entering heat exchanger 124 of the second combustion stage, the flue gas has a temperature of 1260 ° C. In heat exchanger 124, it is cooled to approx. 45 ° C. and leaves the second combustion stage via line 127 without nitrogen oxide.
  • the energy of a fuel oil flow of 0.00046 kg / s which corresponds to an equivalent energy potential of 20 kW, is to be implemented free of nitrogen oxide and used to heat water to 90 ° C.
  • the 100-degree cracked gas flow (12.98 m3iN / h) is divided in the combustion stage in such a way that 9.73 m3iN / h are conducted into the foot of the annular gap and 3.25 m3iN / h into the head.
  • the air volume of 9.59 m3iN / h required for the combustion flows over the cover plate of the combustion head, warms up by approx. 3 ° C, is mixed with the cracked gas stream, which is led into the foot of the annular gap, and ignited.
  • the gas mixture burns to 17.82 m3iN / h exhaust gas. It emits heat into the combustion chamber head and is mixed here with the remaining cracked gas.
  • the free oxygen from the exhaust gas stream oxidizes with the components of the cracked gas to a total of 20.55 m3iN / h exhaust gas.
  • the exhaust gas is cooled to approx. 43 ° C with condensation.
  • the described gasification / nerburning process releases approximately 35% of the energy contained in the heating oil in the gasification stage and approximately 65% in the combustion stage.
  • the water-cooled walls of the gasification and combustion stage play an important role in the heat dissipation, since together they dissipate approx. 20% of the sensible heat into the water.
  • a third exemplary embodiment of the device is described below with reference to FIG. 1.
  • the CH4 / air mixture flows tangentially through the first line 101 into an approximately 5-30 mm wide and approximately 150-300 mm high ring channel 103, in which it is ignited in the foot with a spark plug 102.
  • the flue gas then flows into the head of the ring channel 103 while cooling.
  • the flue gas mixes with the CH4, which is fed in via a perforated plate 106, then passes through the inlet opening 109 into the Mixing space 110 and then flows through the catalyst 111.
  • Both the mixing space 109 and the catalyst 111 have a diameter of 100-150 mm.
  • the heat exchanger 114 of the 1st combustion stage consists of smooth tubes in the region of the gas temperatures of over 700 ° C., and finned tubes in the temperature range below.
  • the flame length is kept very short, so that an empty flame / blasting space is dispensed with and the first layer of smooth tubes can therefore be installed about 10 mm behind the catalyst.
  • a partial stream of the cracked gas is branched off, mixed with air and conducted and ignited in the base of the 5-30 mm wide and 150-300 mm high ring channel.
  • the first gas inflow lines 101 (1st stage) and 116 (2nd stage) are each equipped with flame arresters.
  • the flow and mixing path of the gas in the 2nd combustion stage is identical to that in the 1st combustion stage.
  • the dimensions of the annular or gap-shaped combustion chamber, the admixture of the remaining cracked gas, the mixing device and the catalyst are also kept approximately identical to those of the 1st combustion stage.
  • the design criteria for the second stage heat exchanger 124 are the same as for the first stage heat exchanger 114, i.e. in the area of gas temperatures over 700 ° C smooth tubes, then finned tubes.
  • the catalytic combustion and the associated short flame length also allow the 1st smooth tube layer to be installed approx. 10 mm behind the catalytic converter.
  • the air for the gasification stage flows through the cover hood, which has a diameter of 150 mm, and passes through a pipe, NW 40, into the foot of the annular gap with an outer diameter of 169 mm and an inner diameter of 152 mm. From here, the air passes the flame arrester, which holds about 40% of the free annular space with its holes.
  • the catalyst system which consists of three individual catalyst blocks, each 30 mm deep and 100 mm in diameter.
  • the boundary to the flame space is formed by a storage plate, which reflects 50% of the oil when it hits the flame space, but lets the other 50% through a fine hole of approx. 1 mm.
  • the external dimensions of this storage plate correspond to those of a catalyst block.
  • the cracked gas flows through a cooler with a diameter of 159 mm and a length of 230 mm, the water to be heated on the jacket side and the gas on the pipe side flowing through 121 pipes, NW 10.
  • the gas flows from bottom to top through an empty train with the dimensions 200 x 180.
  • part of the cracked gas regulated by a butterfly valve, is fed into the head of the combustion cable through a NW 40 pipe.
  • the remaining cracked gas at the end of the empty train is also removed through a pipe NW 40, mixed with the air that is sucked in through the cover, ignited and passed into the annular gap of the combustion part, which has the same dimensions as that of the cracked gas generation part.
  • the mixture with the cracked gas and the conversion to exhaust gas takes place in the catalyst system, which is identical to that of the cracked gas generating part. Only the storage plate is replaced by an additional catalyst block.
  • the exhaust gas is cooled in a heat exchanger system.
  • This system consists of three individual heat exchangers, each with the same dimensions and the same structure as the heat exchanger for cracked gas cooling.
  • the heat exchange itself takes place in counterflow.
  • the exhaust gases are drawn off via a pipe NW 40 via a blower, which generates a vacuum of 50 mmWS, and fed into the chimney.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
EP86900771A 1985-02-01 1986-01-29 Vorrichtung zur verbrennung von flüssigen und gasförmigen brennstoffen mit stickoxidfreien abgasen Expired - Lifetime EP0210205B1 (de)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT86900771T ATE58219T1 (de) 1985-02-01 1986-01-29 Vorrichtung zur verbrennung von fluessigen und gasfoermigen brennstoffen mit stickoxidfreien abgasen.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE3503413 1985-02-01
DE19853503413 DE3503413A1 (de) 1985-02-01 1985-02-01 Verfahren und vorrichtung zur vierstufigen verbrennung von gasfoermigen und fluessigen brennstoffen mit stickoxidfreien abgasen

Publications (2)

Publication Number Publication Date
EP0210205A1 EP0210205A1 (de) 1987-02-04
EP0210205B1 true EP0210205B1 (de) 1990-11-07

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EP86900771A Expired - Lifetime EP0210205B1 (de) 1985-02-01 1986-01-29 Vorrichtung zur verbrennung von flüssigen und gasförmigen brennstoffen mit stickoxidfreien abgasen

Country Status (4)

Country Link
US (1) US4725222A (enrdf_load_stackoverflow)
EP (1) EP0210205B1 (enrdf_load_stackoverflow)
DE (1) DE3503413A1 (enrdf_load_stackoverflow)
WO (1) WO1986004662A1 (enrdf_load_stackoverflow)

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DE3636024A1 (de) * 1986-10-23 1988-05-05 Rheinische Braunkohlenw Ag Kraftwerksprozess mit einer gasturbine
DE4438356C2 (de) * 1994-10-27 1997-04-30 Ruhrgas Ag Verfahren und Vorrichtung zur zweistufigen Verbrennung von gas- oder dampfförmigem Brennstoff
EP0821196B1 (de) * 1996-07-26 2003-01-02 Forschungszentrum Karlsruhe GmbH Verfahren und Vorrichtung zur NOx- armen Verbrennung stickstoffhaltiger, organischer und anorganischer Spezies
GB2326934A (en) * 1997-07-01 1999-01-06 Drax Torches Ltd Burners
US6776606B2 (en) * 2001-03-02 2004-08-17 Emmissions Technology, Llc Method for oxidizing mixtures
US20040255874A1 (en) * 2003-04-14 2004-12-23 James Haskew Method and system for increasing fuel economy in carbon-based fuel combustion processes
US8033167B2 (en) * 2009-02-24 2011-10-11 Gary Miller Systems and methods for providing a catalyst
US9939153B2 (en) * 2013-06-03 2018-04-10 Washington University Method and apparatus for capturing carbon dioxide during combustion of carbon containing fuel
EP3247953A4 (en) * 2014-12-30 2018-11-14 Washington University Radiant boiler for pressurized oxy-combustion and method of radiant trapping to control heat flux in high temperature particle-laden flows at elevated pressure
US11555612B2 (en) * 2017-11-29 2023-01-17 Babcock Power Services, Inc. Dual fuel direct ignition burners
US11029020B2 (en) 2018-06-04 2021-06-08 Washington University Oxy-combustion process with modular boiler design
CN114508898B (zh) * 2022-01-27 2023-06-30 广州兴丰能源科技有限公司 一种化工用天然气液化的冷箱预冷设备

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US2205554A (en) * 1935-12-16 1940-06-25 Combustion Utilities Corp Method for generating oil gas
US3982879A (en) * 1971-05-13 1976-09-28 Engelhard Minerals & Chemicals Corporation Furnace apparatus and method
US4161164A (en) * 1972-07-17 1979-07-17 Siemens Aktiengesellschaft Internal combustion engine fuel supply system
US4131086A (en) * 1974-07-20 1978-12-26 Nippon Soken, Inc. Fuel reforming apparatus for use with internal combustion engine
US3948223A (en) * 1975-01-02 1976-04-06 Foster Wheeler Energy Corporation Serially fired steam generator
GB1496116A (en) * 1976-06-24 1977-12-30 United Stirling Ab & Co Method and an apparatus for burning hydrocarbon fuel
US4395223A (en) * 1978-06-09 1983-07-26 Hitachi Shipbuilding & Engineering Co., Ltd. Multi-stage combustion method for inhibiting formation of nitrogen oxides
US4354821A (en) * 1980-05-27 1982-10-19 The United States Of America As Represented By The United States Environmental Protection Agency Multiple stage catalytic combustion process and system
FR2551183B1 (fr) * 1983-05-20 1988-05-13 Rhone Poulenc Chim Base Procede et dispositif de combustion propre s'appliquant notamment au brulage des combustibles lourds
DE3332572C2 (de) * 1983-09-09 1986-10-30 Insumma Projektgesellschaft mbH, 8500 Nürnberg Brennwertgerät für Kohlenwasserstoffe
EP0145920B1 (de) * 1983-11-03 1990-02-07 KAT-TEC Gesellschaft für Katalysatortechnik mbH Verbrennungsvorrichtung

Also Published As

Publication number Publication date
EP0210205A1 (de) 1987-02-04
DE3503413A1 (de) 1986-08-07
DE3503413C2 (enrdf_load_stackoverflow) 1993-08-19
WO1986004662A1 (en) 1986-08-14
US4725222A (en) 1988-02-16

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