EP0017891A2 - 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

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Publication number
EP0017891A2
EP0017891A2 EP80101854A EP80101854A EP0017891A2 EP 0017891 A2 EP0017891 A2 EP 0017891A2 EP 80101854 A EP80101854 A EP 80101854A EP 80101854 A EP80101854 A EP 80101854A EP 0017891 A2 EP0017891 A2 EP 0017891A2
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EP
European Patent Office
Prior art keywords
methanol
oxygen
weight
combustion
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.)
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EP80101854A
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German (de)
English (en)
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EP0017891B1 (fr
EP0017891A3 (en
Inventor
Peter Dr. Schuchart
Wolfgang Muehlthaler
Hans Dr. Diem
Christian Dr. Dudeck
Gunter Lehmann
Albrecht Aicher
Alfred Dr. Stoeckel
Gerd Hemmer
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BASF SE
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BASF SE
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Publication of EP0017891A2 publication Critical patent/EP0017891A2/fr
Publication of EP0017891A3 publication Critical patent/EP0017891A3/de
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Publication of EP0017891B1 publication Critical patent/EP0017891B1/fr
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    • 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 producing 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 incompletely burning the methanol in the flame formed in the presence of certain amounts of water vapor.
  • combustion gases are burned in the form of mixtures of air and gaseous or liquid hydrocarbons, for example methane, benzene, gasoline, and the combustion gases thus obtained are used as heating gases.
  • These combustion gases practically always contain certain amounts of soot; in particular, soot forms when the hydrocarbons are incompletely burned (Ullmanne, loc. cit., volume 14, pages 793, 794; Hoffmann, Inorganic Chemistry (Vieweg, Hraunschweig, 10th edition), page 330).
  • Soot is finely divided carbon that can still contain oxygen, hydrogen and to a lesser extent sulfur, nitrogen and by-products.
  • soot-containing combustion gases can contain up to 10% by weight of soot, based on the weight of the hydrogen carbonate used.
  • soot separation also brings with it other operational difficulties, such as increased cleaning costs for systems and pipe connections, clogging of valves or pipe constriction gene and thus malfunctions, impairment of chemical reactions due to the presence of soot or reduction in activity or poisoning of catalysts.
  • DE-PS 22 24 223 describes a process for the production of soot-free or soot-free combustion gases at 400 to 1 300 ° C, wherein a starting mixture of methanol and oxygen in a ratio of 1 to 10 weight percent 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 produced ignites and 85 to 99 percent by weight in the flame formed the total amount of 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 is used in liquid form
  • the process 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, for example 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 reaction 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 also has to be specially cleaned for some syntheses, for example the aforementioned formaldehyde production.
  • Air as heating gas is out of the question for syntheses in which air components could form explosive mixtures in the later reaction, for example in reactions with alkanols.
  • Luminous gas and town gas result in heating gases which, in addition to soot, also contain sulfur in particular and thus 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.
  • the catalyst becomes quick and uniform. brought to the desired temperature and reduced the usual heating time.
  • the method according to the invention is simpler and more economical; Mixing, regulating and control devices are saved because, 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. If the same quantities of heating gas are produced every hour, the invented value is combustion chamber according to the invention 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. 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 weight percent 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 at such a pressure, for example in the case of oxygen or air, expediently from 1 to 6, in particular from 1.01 to 2.5 bar, that the aforementioned weight ratios and flow velocities of the starting mixture occur 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-AS 12 77 834 and DP 12 35 881, can also be used.
  • the inlet mixing nozzle or the feed of the methanol into the oxygen (air) stream is expediently within a range of 2 centimeters from the inlet of the burner chamber.
  • the mixture thus formed is ignited in a known manner, for example by means of electrical sparks from 5,000 to 20,000 volts.
  • the ignition temperature of the final mixture is between 400 and 500 o C.
  • a soot-free or soot-free flame is formed and generally a combustion temperature of 600 to 1,600 ° C, preferably 650 to 1,500 ° C (measured at the end of the flame cone ).
  • the heat of combustion is appropriately 1,400 to 3,200 kJ / Nm 3 . It is advantageous to adjust the flame cone so that the distance (cone height) from the tip of the cone 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. If air is used as the oxidizing agent, or crude methanol as the starting material, as is commercially interesting, the corresponding proportions of noble gases, such as argon, or impurities, such as dimethyl ether, ammonia, monomethylamine, are also contained in the gas mixture.
  • noble gases such as argon
  • impurities such as dimethyl ether, ammonia, monomethylamine
  • the combustion chamber contains the ignition device at the head and is expediently rectangular 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 1,000 perforations, perforation diameters 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 of 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 inventive are advantageous. Combustion gases used to heat silver catalysts that catalyze the conversion of methanol with oxygen to formaldehyde.
  • the silver catalyst does not become poisoned.
  • This procedure can also be carried out in one step up to the reaction temperature or in two steps, at a lower starting temperature and then at the reaction temperature.
  • the flow rate is advantageously 50 to 1,000 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.
  • 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 the formaldehyde synthesis evenly over the surface of 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, in particular when heating, for example formation of inactive areas, soot formation, sintering due to overheating and impairment of the activity of the catalyst are avoided.
  • 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 2 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 is the uniform distribution of the combustion gases over the entire surface of the catalyst layer causes.
  • the baffles are appropriately similar to the show! arranged by 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, for example the processes for the production of formaldehyde described in Ullmanns Encyklopadie der Technische Chemie, Volume 7, pages 659 ff.
  • 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-AS 12 77 834 and DP 12 35 881, 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 appropriately 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 advantageously 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, for example those described in German Ausletschrift 12 31 229 and Ullmanns Encyklopadie der Technische Chemie, Volume 7, pages 659 ff.
  • Two-layer or multilayer silver catalysts are preferably used; For example, that in the German Ausleschrift 12 94 360, in the German Laid-open specification 19 03 197 or catalysts listed in German specification 23 22 757. With regard to the preparation of the catalyst and implementation of the corresponding reaction with these catalysts, reference is made to the publications mentioned.
  • the oxidation is otherwise carried out in a known manner, for example by a gas mixture of methanol vapor, water vapor, air, optionally inert gas and exhaust gas, in the aforementioned amounts at temperatures of about 550 to 750 ° C, in particular 600 to 700 ° C, through the silver catalyst directs.
  • the process is generally carried out continuously at pressures between 0.5 and 2 bar, preferably between 0.8 and 1.8 bar.
  • reaction gases leaving the catalyst zone it is expedient to cool the reaction gases leaving the catalyst zone within a short time, for example in less than 1/10 seconds, for example to temperatures of 350.degree.
  • the cooled gas mixture is then expediently fed to an absorption tower in which the formaldehyde is washed out of the gas mixture with water, advantageously in countercurrent.
  • the ignition and combustion is carried out in the following combustion chamber (see drawing):
  • the combustion chamber (l) 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 is 50 centimeters
  • the inside tel (6) is perforated from 24 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 feed (7) is 0.7 centimeters above the chamber entrance (9).
  • the heat of combustion is 3,000 kJ / Nm 3 .
  • the gas mixture mixes with 300 parts of water vapor per hour (flow rate 20 meters per second; temperature 120 ° C), which enters 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 mounted in the head of the reactor (13) containing the silver catalyst, via a two-layer catalyst in Reactor (13) passed, the lower layer of the catalyst being 25 millimeters thick and consisting of 90 percent by weight of crystals with a grain size of 1 to 2.5 millimeters and the upper layer with a thickness of 1.5 millimeters and crystals with a grain size 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.

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  • 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)
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 true EP0017891A2 (fr) 1980-10-29
EP0017891A3 EP0017891A3 (en) 1980-12-10
EP0017891B1 EP0017891B1 (fr) 1982-12-08

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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

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

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1154201A2 (fr) * 2000-05-11 2001-11-14 Tribovent Verfahrensentwicklung GmbH Dispositif pour la production de gaz chaud de pulvérisation

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2224223B2 (de) * 1972-05-18 1975-03-06 Basf Ag, 6700 Ludwigshafen Verfahren zur Herstellung von rußfreien oder ruBarmen Verbrennungsgasen
GB2001161A (en) * 1977-07-15 1979-01-24 Zink Co John Steam injection to zone of conset of combustion in fuel burner

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2224223B2 (de) * 1972-05-18 1975-03-06 Basf Ag, 6700 Ludwigshafen Verfahren zur Herstellung von rußfreien oder ruBarmen Verbrennungsgasen
GB2001161A (en) * 1977-07-15 1979-01-24 Zink Co John Steam injection to zone of conset of combustion in fuel burner

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1154201A2 (fr) * 2000-05-11 2001-11-14 Tribovent Verfahrensentwicklung GmbH Dispositif pour la production de gaz chaud de pulvérisation
EP1154201A3 (fr) * 2000-05-11 2002-01-09 Tribovent Verfahrensentwicklung GmbH Dispositif pour la production de gaz chaud de pulvérisation

Also Published As

Publication number Publication date
GR66813B (fr) 1981-04-30
EP0017891B1 (fr) 1982-12-08
EP0017891A3 (en) 1980-12-10
DE2914700A1 (de) 1980-10-30
DE3061252D1 (en) 1983-01-13

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