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WO1988001253A1 - Procede de production de gaz riche en dioxyde d'azote ou d'oxygene pur - Google Patents

Procede de production de gaz riche en dioxyde d'azote ou d'oxygene pur Download PDF

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Publication number
WO1988001253A1
WO1988001253A1 PCT/EP1987/000442 EP8700442W WO8801253A1 WO 1988001253 A1 WO1988001253 A1 WO 1988001253A1 EP 8700442 W EP8700442 W EP 8700442W WO 8801253 A1 WO8801253 A1 WO 8801253A1
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Prior art keywords
oxygen
gas
nitrogen
stage
temperature
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PCT/EP1987/000442
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German (de)
English (en)
Inventor
Zbigniew Boguslawski
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Classifications

    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B21/00—Nitrogen; Compounds thereof
    • C01B21/20—Nitrogen oxides; Oxyacids of nitrogen; Salts thereof
    • C01B21/38—Nitric acid
    • C01B21/40—Preparation by absorption of oxides of nitrogen
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B13/00—Oxygen; Ozone; Oxides or hydroxides in general
    • C01B13/02—Preparation of oxygen
    • C01B13/0229—Purification or separation processes
    • C01B13/0248—Physical processing only
    • C01B13/0259—Physical processing only by adsorption on solids
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B13/00—Oxygen; Ozone; Oxides or hydroxides in general
    • C01B13/10—Preparation of ozone
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B21/00—Nitrogen; Compounds thereof
    • C01B21/04—Purification or separation of nitrogen
    • C01B21/0405—Purification or separation processes
    • C01B21/0433—Physical processing only
    • C01B21/045—Physical processing only by adsorption in solids
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B21/00—Nitrogen; Compounds thereof
    • C01B21/20—Nitrogen oxides; Oxyacids of nitrogen; Salts thereof
    • C01B21/36—Nitrogen dioxide (NO2, N2O4)
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B25/00—Phosphorus; Compounds thereof
    • C01B25/16—Oxyacids of phosphorus; Salts thereof
    • C01B25/18—Phosphoric acid
    • C01B25/22—Preparation by reacting phosphate-containing material with an acid, e.g. wet process
    • C01B25/2208—Preparation by reacting phosphate-containing material with an acid, e.g. wet process with an acid or a mixture of acids other than sulfuric acid
    • C01B25/2216—Preparation by reacting phosphate-containing material with an acid, e.g. wet process with an acid or a mixture of acids other than sulfuric acid with nitric acid or nitrous vapours in aqueous medium
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B7/00—Halogens; Halogen acids
    • C01B7/01—Chlorine; Hydrogen chloride
    • C01B7/03—Preparation from chlorides
    • C01B7/035—Preparation of hydrogen chloride from chlorides
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02B—INTERNAL-COMBUSTION PISTON ENGINES; COMBUSTION ENGINES IN GENERAL
    • F02B43/00—Engines characterised by operating on gaseous fuels; Plants including such engines
    • F02B43/10—Engines or plants characterised by use of other specific gases, e.g. acetylene, oxyhydrogen
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02T—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO TRANSPORTATION
    • Y02T10/00—Road transport of goods or passengers
    • Y02T10/10—Internal combustion engine [ICE] based vehicles
    • Y02T10/30—Use of alternative fuels, e.g. biofuels

Definitions

  • the invention relates to a process for the production of nitrogen oxide rich gas (N02 rich gas) for example for the production of hydroxylamine or nitric acid and / or useful gas with a high content of oxygen or nitrogen.
  • N02 rich gas nitrogen oxide rich gas
  • the manganese dioxide is not soluble in nitric acid, whereas the water-soluble nitrogen oxides (N203) easily dissolve manganese dioxide in water-soluble slurries, which have the reduction properties associated with nitrogen monoxide.
  • the N02 rich gas thus becomes a competitor for nitric acid.
  • the present invention is accordingly based on the object of creating a method by means of which nitrogen dioxide gas can be produced in a high concentration in a simple manner.
  • NOx nitrogen oxide
  • the great technical-economic advantage of this process is primarily that the N02 rich gas is an alternative to nitric acid as a cheap waste product and, depending on the type and method of production, has a 30 to 70% lower market price.
  • the methods that could be implemented with Salpet 5 acid for technical reasons are fa had to be left.
  • This includes, for example, the chlorine production method from waste salts such as NaCl, CaC12, MgC12 waste hydrochloric acid.
  • the invention provides a method by means of which H nitrogen oxide (NOx) is concentrated to a high proportion of nitrogen dioxide regardless of the concentration in the starting gas.
  • K The concentration takes place without any other material consumption insofar as the required intermediate carrier material can be recovered without loss and can be used indefinitely as an intermediate carrier material .
  • NOx nitrogen oxide
  • K The concentration takes place without any other material consumption insofar as the required intermediate carrier material can be recovered without loss and can be used indefinitely as an intermediate carrier material .
  • possibly in divalent form - as NO - existing nitrogen is oxidized into the tetravalent form, so that. the resulting gas, regardless of the N0 / N02 ratio in the starting gas, is almost pure nitrogen dioxide gas in - as a further advantage over the known process - is obtained in dry form.
  • the method of the invention in modifications) the possibility of obtaining concentrated oxygen and / or nitrogen gases within the scope of nitrogen dioxide enrichment, whereby these methods can also be used independently of nitrogen dioxide enrichment
  • the generation stage of the deoxidation stage is preceded as a separate heat treatment stage at a temperature between 80 ° and 150 ° C.
  • the upstream regeneration stage takes place Expulsion of the nitrogen dioxide with the formation of manganese dioxide and the heat treatment or deoxidation stage (200-450 ° C.), the recovery of the dimanganese trioxide from the manganese dioxide with release of oxygen.
  • the use of any kind of nitrogen oxide-containing Ga is possible, the present method with excellent results also for cleaning nitrogen oxide-contaminated Gases can be used.
  • the higher proportion of nitrogen oxide-containing process gases of the catalytic ammonia dispersion can be used as nitrogen oxide-containing gases, as can the exhaust gas containing only small amounts of nitrogen oxide. Flue gases from internal combustion engines or engines or exhaust gases from domestic heating, industrial furnaces or the like, which are also subject to a practically quantitative cleaning of the highly toxic harmful gas components.
  • oxygen which accumulates in the deoxidation stage can be used for oxygenation of the combustion air in the combustion engine, as a result of which a not inconsiderable enrichment of the combustion air of up to 5% and more can be achieved.
  • the disadvantages for the combustion of such machines can be countered with great success by one for the combustion - S " -
  • Exhaust gas purification for the production of pure oxygen and re nitrogen or - in internal combustion engines or engines - z preventive pollutant reduction in such a way that immediately atmospheric oxygen at a temperature between 300 ° and 450 ° C is added to dimanga trioxide (chemisorbed) and the sorbate formed is desorbed by heat treatment at 480 ° - 560 ° C.
  • the heat treatment of the deoxidation stage can be carried out in a pure oxygen atmosphere and under increased pressure between 10 and 200 atm. It has surprisingly been found that under these process conditions in the deoxidation stage by atomically developing oxygen in an extraordinarily simple and cost-saving manner with high performance ozone can be produced, which previously requires considerable investment and process on the way of electrical discharges must become.
  • the _ formed N02 rich gas * can be used in a variety of ways, such as in a manner known per se for the production of nitric acid or mixed acid from nitric acid and sulfuric acid by simply introducing the statu nascendi, released by heat treatment or released from the Liquid phase evaporated N02 rich gas in. What ser, further for the production of hydroxylamine or for the nitration of organic or inorganic compounds.
  • the nitrogen dioxide formed can be used according to the invention with particular advantage for the digestion of insoluble phosphates, in particular calcium phosphate, in such a way that the N02 rich gas formed is introduced into a suspension of finely ground calcium phosphate and the solution formed to crystallize the calcium nitrate to a temperature is cooled below 10 ° C. It is possible in this simple manner to break down insoluble calcium phosphate into phosphoric acid and calcium nitrate, which can be used in large quantities as fertilizer. -? -
  • the procedure can also be carried out in such a way that, simultaneously with the N02 enrichment.
  • N02 rich gas the production of chlorine gas, alkali or alkaline earth metal chlorides, preferably from the masses of sodium, potassium, magnesium, calcium and ammonium chlorides accumulating as waste products, takes place.
  • the stic oxide-containing gas is advantageous.
  • N02-Reichgas together with oxidizing oxygen introduces a slurry of manganese dioxide containing the metal halide and the nitrate solution formed with the elimination of chlorine gas is dried by spray drying at 200 ° to 300 ° C with (re) recovery of N02-Reichg and the mixture formed for washing out the Alkali or alkaline earth metal nitrates is slurried.
  • This method according to the invention is based on the knowledge that the manganese dioxide oxidizes the nitrogen ox to a complex corresponding to the formula N203, which, respectively, removes chlorine gas from the metal chloride and both with the alkali. Form alkaline earth metal as well as with the manganese nitrates, which can be worked up in the manner specified.
  • the nitrate obtained in this way for example from sodium or potassium chloride, can be used directly as a fertilizer.
  • alkali or Alkaline earth metal chlorides which form when the nitrate decomposes below 300 ° C., for example sodium nitrate, are expediently separated from the manganese nitrate by fractional crystallization before the spray drying.
  • Both the nitrates obtained in the manner described above and those obtained naturally can also be chemically worked up to NO2 rich gas using dianthan trioxide. 'S'
  • the treatment of the nitrogen oxide-containing gases can be carried out in reactors connected in parallel or in series such that the reactors alternate with nitrogen oxide absorption and heat treatment.
  • the treatment of the nitrogen oxide-containing gases is carried out in series-connected reactors, the masses being rinsed in the regeneration stage with steam or oxygen heated to 480 ° to 560 ° C. and the gas thus formed after cooling and removal dried from nitrogen oxide residues and then pressurized for the purpose of condensing oxygen.
  • a gas which is highly enriched with oxygen and which can be used for the production of liquid oxygen can be produced in the simplest way.
  • the sorption takes place in two stages such that in the first stage the essential part of the nitrogen oxide and in the second stage the residual nitrogen oxide and residual oxygen are absorbed. It is possible in this extraordinarily simple way to produce technical nitrogen, which is present in practically pure form after the second absorption stage and can be further processed after drying to liquid nitrogen or in any other manner.
  • dimanganese trioxide is possible in any way.
  • the treatment is particularly advantageously carried out using v to pellet agglomerated dimanganese trioxide mass from a mixture of 4 60 wt .-% manganese dioxide, about 2.5 wt .-% sand, about 15 wt .-% cement, b to 3 wt .-% bentonite, 15-20 wt .-% Sawdust and / or plastic granules with a grain size of less than 20 millimeters and 10 to 12 percent by weight pelletizing water agglomerate and gradually increase after the agglomeration for two hours at temperatures of about 50 °, 100 ° and 150 ° C and then again for a period of have been heat treated for two hours each with a temperature between 350 ° and 500 ° C and in a continuously flowing air stream 53 and 580 ° C.
  • the treatment of the green pellets is carried out after 8 to 72 hours of lying in chutes under 20 cm.
  • 1 shows a plant for the concentration of nitrogen dioxide-containing gas and the production of nitric acid
  • Fig. 3 shows another embodiment of a device for enrichment tion of the supply air of internal combustion engines with oxygen
  • Fig. 4 shows a plant for the production of ozone
  • Fig. 6 is a plant for processing waste metal chlorides, A fall hydrochloric acid or ammonium chloride to chlorine - to -
  • a furnace 1 for the catalytic combustion of ammonia, in its place any other arbitrary nitrogen oxide source, for example the exhaust pipe of a nitric acid production plant, an internal combustion engine , a boiler or the like.
  • the furnace 1 is a cooler 2 and connected via a line two by series connection to a double absorber unit verbu dene absorbers 4, 5.
  • a double absorber unit verbu dene absorbers 4, 5 Appropriately, however, two double absorber units connected in parallel to one another or three absorbers connected in series are provided which alternately or respectively. in the Ural run.
  • Another line 6 branches off in front of the cooler 2 and likewise leads to the absorber units 4, 5. Via this line uncooled gas is led to the absorbers.
  • the absorbers are followed by a nitrogen dioxide absorption column 7.
  • furnace 1 is burned with a minimal excess of ammonia and the gas mixture formed after cooling with heat recovery in the cooler 2 is first passed into the first absorber 4, in which the manganese oxide component of the dimangan trioxide contained therein in manganese nitrite / nitrate and any traces of ammonia still present in the gas can be oxidatively destroyed.
  • the gas then passes into the absorber 5, in which it is freed from the remaining traces of nitrogen oxide, but moreover from the remaining oxygen residues. Pure nitrogen remains which, after drying, can be further processed to liquid nitrogen in a known manner.
  • the oxygen-containing N02 rich gas is led into the absorption colon, in which the N02 is dissolved to nitric acid.
  • the remaining oxygen can be used as circulating oxygen or, after liberation of residual nitrogen dioxide, can be worked up to liquid oxygen.
  • d absorber 4 After regeneration and deoxidation of the active mass, d absorber 4 is available for fine cleaning of the combustion gas, so that the absorber unit can now be operated at full power again. Since the regeneration time is extremely short compared to the absorption time (the time ratio is between 1:25 and 1:50, the time of reduced performance is extremely short.
  • This method of operation also enables the production of high-quality oxygen in such a way that when the nitrogen oxide-containing gases are treated in series-connected reactors, the mass is rinsed in the de-oxidation stage with steam or oxygen heated to 480 ° to 530 ° C and the resulting mixture is formed After cooling and releasing nitrogen oxide residues, the gas is dried and then pressurized for the purpose of condensing oxygen. With the aid of this procedure, a gas which is highly enriched with oxygen and which can be used for the production of liquid oxygen can be generated in the simplest way.
  • the inventive method is also excellent z use in motor vehicles, where on the one hand a quantitative purification of the exhaust gases from the nitrogen oxides and carbon monoxide and d hydrocarbons formed and on the other hand an enrichment of the expansion air with oxygen can be achieved.
  • This can be especially Operation of internal combustion engines at high geographical heights or areas prone to smog may be advantageous in which, according to the invention, the air has a below-average oxygen content.
  • FIG. 2 Such an installation is shown in FIG. 2, for example. It consists of three reactors, each of which consists of a reaction chamber 11a, 12a, 13a and a heat exchanger 11b, 12b, 13b and are connected in parallel to an exhaust inlet line 14.
  • each a nitrogen dioxide line 15 an oxygen line and an exhaust line 17, each of which lead to a common collecting device.
  • the oxygen line 16 leads into the air intake line d enn machine.
  • the individual reactors When operating the device, the individual reactors are controlled in such a way that the - in functional order - the first chamber as a deoxidation chamber (reacting from Mn02 to Mn203), the two chambers as a regeneration chamber (decomposition of the nitrates to form Mn02) and the third chamber serves as an absorption chamber (absorption of stic oxides on Mn203).
  • the directly elbow derived exhaust gas is introduced, so that under the high heat v about 500 ° to 530 ° C, the manganese dioxide contained in the reaction chamber 11a with release of Oxygen is reduced to dimangan trioxide.
  • Substance is fed into the combustion air via the oxygen line 16 for the purpose of oxygen enrichment.
  • the exhaust gas then arrives at a temperature between 80 ° and 150 ° C. in the heat exchanger 12b d second reactor and here causes the nitrogen dioxide a to split off the manganese nitrate contained therein, with the formation of manganese dioxide. then finally reaches at a temperature below 80 ° C in the reaction chamber 13 a of the reactor 13, in which the nitrogen oxide is absorbed from the gas in direct contact with the dimethane trioxide.
  • the manipulation lines 18, 19 are used to guide the gas in the specified manner and to supply oxidation air in the stripping phase.
  • D The system is reversed in circulation after each. Consumption of the D mangantrioxids in the para * orptionsgrin in such a manner that the digitizi reduction chamber to the absorption chamber, the previous Austreibungskamm to the reduction chamber and the previous absorption chamber to expel will chamber.
  • the oxygen enrichment takes place independently of the cleaning of the exhaust gas from its nitrogen oxide impurities.
  • the combustion engine 21 is followed by a heat exchanger 22 and upstream of two containers 23, 24 filled with dimangantr oxide, which serve to alternate the combustion air with oxygen.
  • a Te is taken from the combustion air flow supplied via line 25, preheated in the heat exchanger 22 to a temperature of between 20 and 450 ° C. and then passed in the first phase via the lines 26, 27 into the reactor 23.
  • a Te is taken from the combustion air flow supplied via line 25, preheated in the heat exchanger 22 to a temperature of between 20 and 450 ° C. and then passed in the first phase via the lines 26, 27 into the reactor 23.
  • the dimangan trioxide absorbs the oxygen contained in the air by sorption.
  • the remainder, consisting essentially of nitrogen, is discharged into the atmosphere via line 28.
  • the reversal follows in such a way that the reactor 24 is filled with preheated air, while the reactor 23 is heated to a temperature of 480 ° -560 ° by supplying a partial stream of the exhaust gas.
  • the D manganese trioxide of the reactor 23 is desorbed accordingly and gives its oxygen via the line 29 to the combustion air of the engine 21 a
  • the device is expediently set up for a number of cycles between • and 12 changes per hour , which corresponds to a time of 5-10 minutes per cycle.
  • the amounts of the active composition decrease to 1 to 1/12 of the stated amounts.
  • the plant shown in FIG. 4 for ozone production consists of th in this case serving as "ozonizers" 30, 31 reaction units which are equipped with an (electrical) additional heating 32 with the aid of which initially consist essentially of manganese dioxide Reaction mass to temperatures up to 550 ° C, preferably 200 ° to 45 C can be heated.
  • the ozonizers are also connected via a compressor 33 to an oxygen tank (not shown) due to the heating and the high pressure, the manganese dioxide mediates the ozonization of the oxygen flowing through the ozonizer, while providing the atomic radical oxygen in high concentration, which chemical equilibrium of the ozonization reaction is maintained by the cooling of the reaction gas in the cooler 34.
  • the manganese dioxide is converted into dimangan trioxide.
  • the ozone formed is passed into the silica gel absorber 35 and sorbed there.
  • the oxygen is circulated and supplemented from the storage container (not shown).
  • the dimangan trioxide formed in the ozonization reaction is then regenerated with N02 rich gas by carrying out nitration in an absorption stage b 20 ° -80 ° C., followed by a regeneration stage at 80 °-150 ° C.
  • N02 rich gas used for nitration is recovered, which is therefore in circulation g can be led.
  • the ozone production described is simple and inexpensive in comparison with the known position processes which operate on the basis of electrical discharges.
  • two pairs 41 / 43/44 of absorber units are provided - in parallel - which are so functionally connected to one another that the ones in the heat exchanger 45 to 300 ° to 450
  • heated air is passed in succession through two absorbers, of which the first absorber 41 or. 42 of the absorption of the essential part of oxygen from the air and the second absorber 43 respectively. 44 serves to absorb the residual oxygen.
  • the remaining residual gas is pure T, which is fed to the liquefaction plant via the heat exchanger to recover the heat.
  • the expulsion of the stored sow material is also carried out by heat at temperatures above 530 ° C, where the fan 46 promotes oxygen through the heat exchanger 47 and superheater 48 in the reactor and again through the heat exchanger 47 recovery of heat in the liquefaction system.
  • a plant for the production of chlorine gas from example as waste material during potash processing alkaline earth metal halide (MgC12) is reproduced using N02-rich gas, the nitrogen oxide-containing gas bezw.
  • the third nitrate solution is worked up as follows:
  • Solutions which contain metal nitrates which do not thermally decompose at 300 ° C. are worked up by spray drying dryer 53 at temperatures between 200 ° and 300 ° C., the manganese nitrate contained in the solution decomposing into manganese dioxide and nitrogen dioxide a by-products, while the others Metal nitrate ounce remains.
  • the dry product is separated in the separator 54, while the carrier gas is removed by means of the fan after recovery of the NO 2 rich gas.
  • the dry residue containing manganese dioxide and water-soluble metal nitrate is brought into the solution mixer 56, in which d - / 9 -
  • Nitrates are removed.
  • the sludge is conveyed by means of the pump 57 into the chamber filter press 58, in which a concentrated nitrate solution is obtained by filtering, which is used immediately as a fertilizer or can be further processed.
  • a concentrated nitrate solution is obtained by filtering, which is used immediately as a fertilizer or can be further processed.
  • hydrochloric acid titanium acid
  • the nitrate solution is conveyed by means of the pump 52 instead of in the dryer 53 into the crystallizer 59 z fractional precipitation of the manganese nitrate.
  • the substrate wi is then brought into the chamber filter press 61 by means of the pump 60, in which the crystallized fraction is separated from the liquid phase which can be processed to form a fertilizer.
  • the filter residue passes through the diffusion mixer 62 into the spray dryer 53 and is worked up there in the manner described above.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Inorganic Chemistry (AREA)
  • Analytical Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Catalysts (AREA)
  • Treating Waste Gases (AREA)
  • Exhaust Gas Treatment By Means Of Catalyst (AREA)

Abstract

Selon un procédé de production de gaz riche en dioxyde d'azote (gaz riche en NO2), utile dans la production d'acide nitrique ou d'hydroxylamine par exemple, et/ou de gaz de réaction à haute teneur en oxygène ou en azote, un gaz contenant de l'oxyde nitreux (NOx), par exemple des gaz de fumée émis lors de procédés de combustion, est amené sur ou à travers une masse de réaction composée essentiellement de trioxyde de dimanganèse à une température comprise entre 20° et 80°C, et le nitrate de manganèse obtenu est soumis pendant une deuxième étape à un traitement thermique à une température comprise entre 200° et 450° afin de régénérer le trioxyde de dimanganèse. Afin d'obtenir du dioxyde d'azote dépourvu d'oxygène, on peut exécuter des étapes distinctes de séparation et de désoxydation du dioxyde d'azote avec une étape préliminaire à 80°. L'oxygène produit pendant l'étape de désoxydation peut être utilisé pour enrichir en oxygène l'air de combustion, purifiant ainsi les gaz d'échappement de moteurs à combustion. On peut également exécuter centralement, à grande échelle et dans de grandes unités, l'absorption dans un récipient interchangeable situé à proximité du moteur à combustion, et la régénération de l'oxyde de manganèse après la récupération du nitrate de manganèse ainsi produit. Afin d'obtenir de l'oxygène et de l'azote purs, on ajoute de l'oxygène atmosphérique au trioxyde de dimanganèse à une température comprise entre 300° et 450°C, et le sorbat ainsi obtenu est thermiquement désorbé à une température comprise entre 480° et 560°C, libérant ainsi de l'oxygène pur.
PCT/EP1987/000442 1986-08-13 1987-08-12 Procede de production de gaz riche en dioxyde d'azote ou d'oxygene pur Ceased WO1988001253A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DEP3627429.1 1986-08-13
DE19863627429 DE3627429A1 (de) 1986-08-13 1986-08-13 Verfahren zur herstellung von stickstoffdioxid-reichgas

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Publication Number Publication Date
WO1988001253A1 true WO1988001253A1 (fr) 1988-02-25

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WO (1) WO1988001253A1 (fr)

Cited By (1)

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WO1993008121A1 (fr) * 1991-10-21 1993-04-29 Europäische Atomgemeinschaft (Euratom) PROCEDE DE PREPARATION D'HYDROXYLAMINE A PARTIR DE GAZ DE FUMEE CONTENANT DU NO¿x?

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Publication number Priority date Publication date Assignee Title
DE19742319A1 (de) * 1997-09-25 1999-04-08 Zbigniew Dr Ing Boguslawski Herstellung von Flüssig-Druck-Stickstoff direkt aus der atmosphärischer Luft für brennstoffreien Antrieb von mobilen Einheiten

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