EP0017891B1 - Procédé de préparation de gaz de combustion ne contenant pas de suie ou une faible quantité de suie - Google Patents

Procédé de préparation de gaz de combustion ne contenant pas de suie ou une faible quantité de suie Download PDF

Info

Publication number
EP0017891B1
EP0017891B1 EP80101854A EP80101854A EP0017891B1 EP 0017891 B1 EP0017891 B1 EP 0017891B1 EP 80101854 A EP80101854 A EP 80101854A EP 80101854 A EP80101854 A EP 80101854A EP 0017891 B1 EP0017891 B1 EP 0017891B1
Authority
EP
European Patent Office
Prior art keywords
methanol
combustion
oxygen
weight
mixture
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
Application number
EP80101854A
Other languages
German (de)
English (en)
Other versions
EP0017891A3 (en
EP0017891A2 (fr
Inventor
Peter Dr. Schuchart
Wolfgang Muehlthaler
Hans Dr. Diem
Christian Dr. Dudeck
Gunter Lehmann
Albrecht Aicher
Alfred Dr. Stoeckel
Gerd Hemmer
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.)
BASF SE
Original Assignee
BASF SE
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 BASF SE filed Critical BASF SE
Publication of EP0017891A2 publication Critical patent/EP0017891A2/fr
Publication of EP0017891A3 publication Critical patent/EP0017891A3/de
Application granted granted Critical
Publication of EP0017891B1 publication Critical patent/EP0017891B1/fr
Expired legal-status Critical Current

Links

Images

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
    • F23L7/00—Supplying non-combustible liquids or gases, other than air, to the fire, e.g. oxygen, steam
    • F23L7/002—Supplying water
    • F23L7/005—Evaporated water; Steam
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas

Definitions

  • the invention relates to a process for the production of soot-free or low-soot combustion gases by mixing oxygen of a certain flow rate with liquid methanol in a certain weight ratio, igniting the mixture thus produced and incomplete combustion of the methanol in the flame formed in the presence of certain amounts of water vapor.
  • soot-containing combustion gases can contain up to 10 percent by weight of soot, based on the amount by weight of the hydrocarbon used.
  • soot separation also brings with it other operational difficulties, e.g. B. increased cleaning costs of systems and pipe connections, blockage of valves or pipe constrictions and thus malfunctions, impairment of chemical reactions due to the presence of soot or reduction in activity or poisoning of catalysts.
  • DE-B-2224223 describes a process for the production of soot-free or low-soot combustion gases at 400 to 1300 ° C., wherein a starting mixture of methanol and oxygen in a ratio of 1 to 10 percent by weight oxygen, based on methanol, and a flow rate of 50 to 500 meters per second mixed with oxygen at a flow rate of 1 to 20 meters per second in a ratio of 10 to 80 percent by weight of additional oxygen, based on the starting mixture, the final mixture thus ignited and 85 to 99 percent by weight of the total amount in the flame formed Methanol burns.
  • the combustion is carried out in a kiln which contains the feed lines of the starting mixture and the additional oxygen as well as corresponding ignition devices and the discharge of the combustion gases.
  • soot-free or low-soot combustion gases can be obtained advantageously by igniting a mixture of oxygen and methanol and burning 85 to 99 percent by weight of the total amount of methanol in the flame formed, if methanol in liquid form with oxygen from a flow rate of 1 to 100 meters per second in a ratio of 50 to 150 weight percent oxygen, based on methanoi, mixes, the mixture ignites in a perforated combustion chamber, burns and with through the perforations of the combustion chamber in a ratio of 10 to 3000 weight percent water , based on methanol entering water vapor mixes.
  • the method according to the invention provides soot-free or low-soot combustion gases in a simple and economical way, generally without any detectable soot content.
  • the combustion gases can also be used advantageously as heating gases in all cases in which soot deposition would interfere, e.g. B. for heating oxidic catalysts such as oxides of iron, molybdenum, cobalt, nickel, tungsten, aluminum, titanium, phosphorus and chromium. They can advantageously be used to heat catalysts in catalytic synthesis processes, for example silver catalysts, which catalyze the conversion of methanol with oxygen to formaldehyde.
  • heating gases are also of particular interest in industries or areas where other starting materials for the production of combustion gases, such as benzene or gasoline, or nitrogen as heating gas are not available in sufficient quantities or are uneconomical.
  • Nitrogen as heating gas must also be used for some syntheses, e.g. B. the above-mentioned formaldehyde production can be specially cleaned.
  • Air as a heating gas is not suitable for syntheses in which air components could form explosive mixtures during the subsequent implementation, e.g. B. in reactions with alkanols.
  • Luminous gas and town gas result in heating gases which, in addition to soot, also contain sulfur in particular and so, for. B. impair or poison numerous catalysts or promote corrosion of the systems.
  • Indirect heating on the other hand, is uneconomical, especially on an industrial scale, and it is not possible to achieve uniform heating to higher catalyst temperatures in this way.
  • electrical heating local heating in the middle of the catalyst bed and soot formation are frequently observed.
  • the method according to the invention provides an economically advantageous and reliable heating gas in a simple manner.
  • formaldehyde production the catalyst is brought quickly and uniformly to the desired temperature and the usual heating-up time is reduced.
  • the method according to the invention is simpler and more economical; Mixing, regulating and control devices are saved since, according to the known method, a starting mixture of methanol and oxygen must first be prepared, which is then only mixed with additional oxygen.
  • the method according to the invention comparatively uses only one burner, while the known method requires two burners, namely a main burner and a secondary burner for the ignition. For this reason, a simpler and more reliable ignition and combustion of the starting mixture is achieved comparatively in the method according to the invention.
  • smaller amounts of air are used to burn the methanol; surprisingly, a practically oxygen-free, soot-free combustion gas without by-products is obtained.
  • the combustion chamber according to the invention is cooled with the aid of the steam flowing in for mixing with the combustion gases; local overheating, which can destroy the burner, is avoided. Since the temperature of the combustion chamber wall is therefore comparatively lower, the design of the combustion chamber jacket is cheaper and simpler. All these advantageous results of the method according to the invention are surprising with regard to the prior art.
  • the incomplete combustion of methanol with air would have been expected to cool the combustion chamber walls and scour the combustion mixture and cause soot to form.
  • the temperature of the heating gas can be adjusted within a wide range by adding water vapor.
  • the combustion chamber according to the invention is smaller and lighter than the known combustion chambers.
  • oxygen-containing mixtures are also advantageously used.
  • Mixers and advantageously nozzles come into consideration as mixing devices, e.g. B. injector mixers, mixing chambers or mixing sections with injectors, jet mixers, swirl chamber nozzles, eccentric nozzles, bundle nozzles, centrifugal pressure nozzles, slot nozzles, flat jet nozzles, hollow nozzles, spiral nozzles.
  • the components methanol and oxygen or air, which form the starting mixture, are expediently introduced into the combustion chamber via corresponding nozzles. It is advantageous to add the methanol into the supplied air shortly before or at the entrance to the combustion chamber via a nozzle (input mixing nozzle). Methanol is added in liquid form; the inlet mixing nozzle advantageously forms a fine, droplet-shaped distribution of the liquid methanol in the oxygen or in the supplied air.
  • the starting mixture has a ratio of 50 to 150, in particular 100 to 140 percent by weight of oxygen, based on methanol, and generally a flow rate of 1 to 100, in particular 8 to 45 meters per second.
  • pressures from 1 to 6, in particular from 1.1 to 2.5, bar are expediently considered.
  • the flow rate of oxygen, advantageously air is 1 to 100, in particular 8 to 45 meters per second.
  • the components are supplied under such a pressure, e.g. B. in the oxygen or air expediently from 1 to 6, in particular from 1.01 to 2.5 bar, that the aforementioned weight ratios and flow rates of the starting mixture at the burner inlet.
  • the components are added at room temperature.
  • Starting materials suitable for the process are pure methanol and technical grade methanol. Crude methanol, which can optionally be purified by treatment with oxidizing agents and / or alkalis by the processes described in DE-B-1 277 834 and DE-C-1 235 881, can also be used.
  • the inlet mixing nozzle or the feed of the methanol into the oxygen (air) stream is advantageously within a range of 2 centimeters from the entrance of the burner chamber.
  • the mixture thus formed is known in a known manner, for. B. ignited by electrical sparks of 5000 to 20 000 volts.
  • the ignition temperature of the final mixture is between 400 and 500 ° C.
  • a soot-free or soot-free flame is formed and generally a combustion temperature of 600 to 1600 ° C, preferably of 650 to 1500 ° C (measured at the end of the flame cone).
  • the heat of combustion is expediently 1400 to 3200 kJ / N M 3 . It is advantageous to adjust the flame cone by regulating the oxygen so that the distance (Cone height) from the cone tip at the entrance to the burner chamber to the end of the cone is 10 to 230 centimeters.
  • the diameter of the cone base or the maximum diameter of the flame cone is advantageously 10 to 60 centimeters.
  • the length of the combustion chamber is advantageously 1.2 to 2 times the flame cone height and the diameter or, in the case of a rectangular combustion chamber, a broad side of the combustion chamber is 1.5 to 2 times the flame cone diameter.
  • the combustion is usually carried out continuously.
  • a total pressure of 1 to 6 bar, preferably of 1.01 to 2.5 bar, is expediently set in the combustion chamber.
  • 1 to 30 grams of methanol are burned per second under the aforementioned preferred conditions of combustion and flame cone design.
  • the gas mixture obtained by the ignition and combustion generally contains 0.01 to 0.3 percent by weight of formaldehyde, 0.01 to 1 percent by weight of methanol, 10 to 16 percent by weight of water (without water optionally contained in the starting mixture), 8 to 19 percent by weight of carbon dioxide, 0 to 5 weight percent carbon monoxide and 58.7 to 66 weight percent nitrogen.
  • the oxidizing agent or crude methanol as the starting material as is of particular interest on a large industrial scale, the corresponding proportions of noble gases, such as argon, or impurities, such as e.g. B. Dimethyl ether, ammonia, monomethylamine.
  • the combustion chamber contains the ignition device at the head and is expediently or advantageously tubular.
  • the walls (tube wall) are perforated along the entire wall length below the ignition device or, advantageously, only from 6 centimeters below the ignition device. Preferred are from 2 to 10,000, in particular from 5 to 1000 perforations, diameter of the perforations from 2 to 20 millimeters, wall length of the combustion chamber from 0.2 to 4.6, in particular 0.6 to 1.5 meters, combustion chamber diameter or wall sides the rectangular, equilateral combustion chamber 0.1 to 1.5, in particular 0.2 to 0.8 meters.
  • the gas mixture is mixed with water vapor, which enters through the perforations at a flow rate of 5 to 50, in particular 10 to 25, meters per second.
  • the perforations can be distributed anywhere on the combustion chamber walls (pipe wall), expediently in a uniform distribution or in a ring.
  • the final mixture of gas and water vapor are the combustion gases; They expediently come out at the end of the combustion chamber opposite the ignition without pressure or under pressure, expediently 1.1 to 2.5 bar, expediently at a flow rate of 3 to 20, in particular 5 to 10 meters per second, and can be carried out without further process steps can be used as heating gas.
  • the combustion chamber is installed in front of a reactor or in particular placed on a vertical reactor.
  • the combustion gases according to the invention are advantageously used for heating silver catalysts which catalyze the conversion of methanol with oxygen to formaldehyde.
  • the silver catalyst does not become poisoned.
  • the flow rate is advantageously 50 to 1000 kg of combustion gases per square meter of catalyst bed cross section and hour; if they are mixed with the starting mixture of the reaction, a ratio of 0.1 to 0.5 parts by weight of oxygen in the starting mixture of the methanol oxidation to one part by weight of combustion gas is expediently chosen. It is advantageous to use a gas distributor in front of the catalyst layer, expediently in the reactor hood of the vertical reactor carrying the catalyst layer, which distributes the combustion gases and / or the starting mixture of formaldehyde synthesis evenly over the surface distributed the catalyst layer.
  • the gas distributor in the upper part of the reactor hood, the silver catalyst is heated evenly across the catalyst cross-section.
  • the known damage to the contact, especially when heating, e.g. B. formation of inactive areas, soot formation, sintering due to overheating and impairment of the activity of the catalyst are avoided.
  • the combustion chamber according to the invention with a gas distributor, the yield of formaldehyde is higher than in the known methods of catalyst heating. It is surprising that the combustion gases do not have any negative effects on the catalyst activity due to condensation of the steam, even at the beginning of the heating period.
  • the interior of the pipe section (interior of the outer jacket) consists of two parts, the interior of the inner jacket (tube core) and the interior (ring rim), which is enclosed by the outer wall of the inner jacket and the inner wall of the outer jacket.
  • a hollow tube core and a ring rim, which is provided with baffle walls, are expedient.
  • the lines of contact of the baffle walls with the outer wall of the inner shell and the inner wall of the outer shell expediently form parallel curves or mostly straight lines with angles between the line of contact and the direction of flow of the incoming combustion gases.
  • the outer regions of the gas stream contain a swirl, the turbulence of which causes the combustion gases to be distributed uniformly over the entire surface of the catalyst layer.
  • the baffles are suitably arranged similar to the blades of axial turbines.
  • the oxidation can be carried out in the preferred combination of the process according to the invention with the methanol oxidation on the silver catalyst by the known processes, e.g. B. perform the process described in Ullmanns Encyklopadie der Technische Chemie, Volume 7, pages 659 ff. For the production of formaldehyde.
  • Starting materials suitable for the oxidation are pure methanol, industrial methanol or advantageously their mixtures with water; the concentration of the aqueous mixtures can suitably vary between 60 and 95 percent by weight, preferably between 70 and 90 percent by weight, of methanol.
  • Crude methanol which can optionally be purified by treatment with oxidizing agents and / or alkalis by the processes described in DE-B-1 277 834 and DE-C-1 235 881, can also be used.
  • the methanol is fed to the reaction space in vapor form and, if appropriate, in a mixture with inert gas.
  • Nitrogen for example, can be used as the inert gas for the oxidation.
  • Both pure oxygen and free oxygen-containing gases, in particular air, can be used as the oxidizing agent.
  • Oxygen and methanol are expediently in a molar ratio of 0.15 to 0.6, in particular 0.15 to 0.5 mol, of oxygen per mol of methanol or methanol and air are expediently in a molar ratio of 1 mol of methanol to 1.4 to 2.9 Mole of air applied.
  • the total volume of water vapor is preferably 0.8 to 1.9 parts by volume per volume of methanol vapor.
  • Any silver catalysts are suitable as catalysts, e.g. B. the described in German Ausleschrift 1 231 229 and Ullmanns Encylklopadie der Technische Chemie, Volume 7, pages 659 ff.
  • two-layer or multilayer silver catalysts e.g. B.
  • the oxidation is otherwise carried out in a known manner by z. B. a gas mixture of methanol vapor, water vapor, air, optionally inert gas and exhaust gas; in the aforementioned quantities at temperatures of about 550 to 750 ° C, in particular 600 to 700 ° C, passes through the silver catalyst.
  • the process is generally carried out continuously at pressures between 0.5 and 2 bar, preferably between 0.8 and 1.8 bar.
  • the ignition and combustion is carried out in the following combustion chamber (see drawing):
  • the combustion chamber (1) contains an outer jacket (2), an air inlet (3), a steam inlet (4), an ignition device (5) and a partially perforated inner jacket ( 6).
  • the methanol supply is in the air supply via a pressure atomizing nozzle (7).
  • the combustion gases emerge from the outlet (8) of the combustion chamber.
  • the height between chamber entrance (9) and chamber exit (8) is 70 centimeters, the diameter of the tubular chamber 50 centimeters, the inner jacket (6) is perforated from 40 centimeters below the ignition to 10 centimeters above the chamber exit (8) with 24 perforations with a perforation diameter of 17 millimeters.
  • the ignition (5) is 0.5 centimeters above the chamber entrance (9)
  • the nozzle outlet of the methanol supply (7) is 0.7 centimeters above the chamber entrance (9).
  • the heat of combustion is 3000 kJ / N M 3.
  • the gas mixture mixes with 300 parts of water vapor per hour (flow rate 20 meters per second; temperature 120 ° C), which occurs through the perforations.
  • the combustion gases in the chamber (temperature 700 ° C; pressure 1.1 bar) emerge from the chamber at the chamber outlet (8) and then have a flow rate of 6 meters per second, a temperature of 650 ° C and a pressure of 1, 1 bar. 530 parts of combustion gases at 650 ° C.
  • the combustion chamber is connected via a pipe (10) to the feed (11) of a methanol / air / water vapor mixture of the formaldehyde synthesis.
  • the combustion is carried out analogously to Example 1 and the combustion gases in a composition analogous to Example 1 via feeds (10) and (11) and a gas distributor (12), which is attached to the head of the reactor (13) containing the silver catalyst, via a two-layer catalyst in Reactor (13) passed, wherein the lower layer of the catalyst is 25 millimeters thick and 90 percent by weight of crystals with a grain size of 1 to 2.5 millimeters and the upper layer has a thickness of 1.5 millimeters and crystals with grain sizes of 0 , 2 to 0.75 millimeters.
  • the throughput is 150 kilograms of combustion gases per square meter of catalyst bed cross section and hour.
  • the catalyst is heated to 330 ° C. within 15 minutes.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Claims (1)

  1. Procédé de préparation de gaz de combustion exempts de suie ou pauvres en suie entre 200 et 1600°C par inflammation d'un mélange d'oxygène et de méthanol et combustion de 85 à 99% en poids de la quantité totale de méthanol dans la flamme formée, caractérisé en ce que l'on mélange le méthanol à l'état liquide et de l'oxygène s'écoulant avec une vitesse de 1 à 100 mètres par seconde dans un rapport de 50 à 150% en poids d'oxygène par rapport au méthanol, on inflamme ce mélange dans une chambre de combustion perforée et pendant que la combustion se déroule, on introduit dans le mélange, à travers les perforations de la chambre de combustion, de 10 à 3000%en poids, par rapport au méthanol, d'eau sous forme de vapeur d'eau.
EP80101854A 1979-04-11 1980-04-08 Procédé de préparation de gaz de combustion ne contenant pas de suie ou une faible quantité de suie Expired EP0017891B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE2914700 1979-04-11
DE19792914700 DE2914700A1 (de) 1979-04-11 1979-04-11 Verfahren zur herstellung von russreien oder russarmen verbrennungsgasen

Publications (3)

Publication Number Publication Date
EP0017891A2 EP0017891A2 (fr) 1980-10-29
EP0017891A3 EP0017891A3 (en) 1980-12-10
EP0017891B1 true EP0017891B1 (fr) 1982-12-08

Family

ID=6068090

Family Applications (1)

Application Number Title Priority Date Filing Date
EP80101854A Expired EP0017891B1 (fr) 1979-04-11 1980-04-08 Procédé de préparation de gaz de combustion ne contenant pas de suie ou une faible quantité de suie

Country Status (3)

Country Link
EP (1) EP0017891B1 (fr)
DE (2) DE2914700A1 (fr)
GR (1) GR66813B (fr)

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
AT408956B (de) * 2000-05-11 2002-04-25 Tribovent Verfahrensentwicklg Einrichtung zur erzeugung eines heissen treibgasstromes

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2224223C3 (de) * 1972-05-18 1975-10-23 Basf Ag, 6700 Ludwigshafen Verfahren zur Herstellung von rußfreien oder rußarmen Verbrennungsgasen
US4152108A (en) * 1977-07-15 1979-05-01 John Zink Company Steam injection to zone of onset of combustion in fuel burner

Also Published As

Publication number Publication date
EP0017891A3 (en) 1980-12-10
DE3061252D1 (en) 1983-01-13
GR66813B (fr) 1981-04-30
EP0017891A2 (fr) 1980-10-29
DE2914700A1 (de) 1980-10-30

Similar Documents

Publication Publication Date Title
EP0991587B1 (fr) Procede et dispositif de reformage autotherme d'hydrocarbures
DE1417796C3 (de) Verfahren zur Herstellung eines wasserstoffreichen Gases
CH627536A5 (de) Verfahren zur durchfuehrung einer kontinuierlichen verbrennung eines kohlenstoffhaltigen brennstoffes.
DE2232506C2 (de) Verfahren und Vorrichtung zur Erzeugung eines durch katalytische Umsetzung von Brennstoff und einem als Sauerstoffträger dienenden Gas zu bildenden Gasgemisches
DE102004055425B4 (de) Mischkammer für einen Reformer sowie Verfahren zum Betreiben derselben
EP2160236A1 (fr) Dispositif et procédé pour réactions catalytiques en phase gazeuse et leur utilisation
EP1239944B1 (fr) Procede et dispositif pour produire un melange homogene constitue d'un hydrocarbure aromatique a l'etat de vapeur et d'un gaz contenant de l'oxygene
CH697265B1 (de) Verfahren zum Erzeugen von Wasserdampf, insbesondere Reinstwasserdampf sowie Dampferzeuger.
EP0017891B1 (fr) Procédé de préparation de gaz de combustion ne contenant pas de suie ou une faible quantité de suie
DE2623686C3 (de) Verfahren zur Entfernung von Stickstoffoxiden aus Abgasen
DE2224223C3 (de) Verfahren zur Herstellung von rußfreien oder rußarmen Verbrennungsgasen
DE2655321C3 (de) Verfahren zur Herstellung von rußarmen und schwefelfreien Verbrennungsgasen
DE2363569A1 (de) Verfahren und vorrichtung zur herstellung von gasen durch unvollstaendige verbrennung von kohlenwasserstoffen
EP3038742A1 (fr) Dispositif et procédé de production d'acétylène et de gaz de synthèse
DE1910125C3 (de) Reaktor zur Herstellung von FurnaceruB
DE2326884A1 (de) Verfahren und vorrichtung zur katalytischen oxydation von ammoniak
EP1462160B1 (fr) Procédé pour la réalisation d' une réaction à haute température , réacteur pour la mise en oeuvre de ce procédé et son utilisation
DE19801761A1 (de) Verfahren und Vorrichtung zur NO¶x¶-armen Verbrennung stickstoffhaltiger organischer und anorganischer Spezies
DE1248624C2 (de) Verfahren zur verhinderung von vorzuendungen in der mischzone bei der herstellung von synthesegas
DE2253385A1 (de) Verfahren und brenner zur synthesegasherstellung
AT214053B (de) Verfahren zur thermisch/katalytischen Umwandlung von gasförmigen oder flüssigen Kohlenwasserstoffen
EP0821196B1 (fr) Procédé et dispositif pour la combustion à faible niveau de NOx des espèces organiques ou inorganiques contenant de l'azote
DE1966995C3 (de) Reaktor zur Herstellung von Furnaceruß (H)
EP2004318B1 (fr) Procede de vaporisation d'un carburant liquide
DE2305491C3 (de) Verfahren zur Herstellung von Furnaceruß

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

PUAL Search report despatched

Free format text: ORIGINAL CODE: 0009013

AK Designated contracting states

Designated state(s): BE CH DE FR GB IT NL

AK Designated contracting states

Designated state(s): BE CH DE FR GB IT NL

17P Request for examination filed

Effective date: 19810516

ITF It: translation for a ep patent filed

Owner name: ING. C. GREGORJ S.P.A.

GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

AK Designated contracting states

Designated state(s): BE CH DE FR GB IT NL

REF Corresponds to:

Ref document number: 3061252

Country of ref document: DE

Date of ref document: 19830113

ET Fr: translation filed
ITTA It: last paid annual fee
PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: FR

Payment date: 19990312

Year of fee payment: 20

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: NL

Payment date: 19990322

Year of fee payment: 20

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: CH

Payment date: 19990325

Year of fee payment: 20

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: GB

Payment date: 19990401

Year of fee payment: 20

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: BE

Payment date: 19990409

Year of fee payment: 20

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: DE

Payment date: 19990428

Year of fee payment: 20

BE20 Be: patent expired

Free format text: 20000408 *BASF A.G.

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: LI

Free format text: LAPSE BECAUSE OF EXPIRATION OF PROTECTION

Effective date: 20000407

Ref country code: GB

Free format text: LAPSE BECAUSE OF EXPIRATION OF PROTECTION

Effective date: 20000407

Ref country code: CH

Free format text: LAPSE BECAUSE OF EXPIRATION OF PROTECTION

Effective date: 20000407

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: NL

Free format text: LAPSE BECAUSE OF EXPIRATION OF PROTECTION

Effective date: 20000408

REG Reference to a national code

Ref country code: CH

Ref legal event code: PL

REG Reference to a national code

Ref country code: GB

Ref legal event code: PE20

Effective date: 20000407

NLV7 Nl: ceased due to reaching the maximum lifetime of a patent

Effective date: 20000408

PLBE No opposition filed within time limit

Free format text: ORIGINAL CODE: 0009261

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT