SE190890C1

SE190890C1 -

Info

Publication number: SE190890C1
Authority: SE
Publication date: 1964-01-01

Description

Uppfinnare: W P Hendal och P Visser Prioritet begiird frtin den 20 full 1961 (Nederkinderna) Uppfinningen avser ett satt enligt patentet 178 150 far framstallning av normalt gasformiga olefiner samt en apparat for sattets utforan.de. Inventors: W P Hendal and P Visser Priority given to 20 full 1961 (Nederkinderna) The invention relates to a set according to the patent 178 150 for the production of normally gaseous olefins and an apparatus for the set's performance.

I patentet 178 150 beskrives ett salt att framstalla normalt gasformiga olefiner, sasom eten, propen och liknande, genom krackning av kolvaten med hjalp av ett varmeOverfOringsmeditun bestaende av ett smalt salt, enligt vilket sat ett kolvate-utgangsmaterial blandat med medrivet smalt salt med h8g hastighet fores genom en rorformig reaktionskammare, reaktionsprodukterna separ eras frail saltet i en separationszon och reaktionsprodukterna darefter utmatas ur separationszonen, varvid hi. a. saltet Ores frau separationszonen till en regenereringszon, i vilken det regenereras genom inverkan av en oxiderande gas och aven upphettas till erforderlig hog temperatur samt saltet slutligen aterinfares tillsammans med kolvate-utgangsmaterialet. Patent 178,150 discloses a salt for producing normally gaseous olefins, such as ethylene, propylene and the like, by cracking the hydrocarbons by means of a heat transfer medium consisting of a narrow salt, according to which a hydrocarbon feedstock is mixed with entrained narrow salt at high speed is passed through a tubular reaction chamber, the reaction products are separated from the salt in a separation zone and the reaction products are then discharged from the separation zone, wherein hi. a. the salt Ores frau the separation zone into a regeneration zone, in which it is regenerated by the action of an oxidizing gas and also heated to the required high temperature and the salt is finally re-inhaled together with the hydrocarbon starting material.

Enligt uppfinningen sker upphettningen av saltet i regenereringszonen pa. ett effektivt satt genom tillfarande av varme frau forbranning av ett vatske- eller gasformigt bransle i en brannare, varvid den smalta saltmassan medtages av forbranningsgaserna i finfordelat till-stand genom ejektorverkan och darefter separeras fran dessa gaser. According to the invention, the salt is heated in the regeneration zone pa. an efficient method by applying heat from the combustion of a liquid or gaseous fuel in a burner, the narrow salt mass being taken up by the combustion gases in the finely divided state by ejector action and then separated from these gases.

Uppfinningen avser vidare en apparat f8r genomforande ax sattet, vilken apparat kanneteclmas darav, att den innefattar en eller flera brannare f5r att till den smalta saltmassan tillfOra det varme, som erfordras for reaktionen, vilken eller vilka brannare aro forsedda med ledning for tillforsel av syre eller syrehaltig gas samt med ledningar for utmatning Dupl. kl. 10 a: 24/04; 12 g: 1/02; 12 o: 27 av farbranningsgaser, varvid brannaren eller brannarna sta. i oppen forbindelse med en kammare fylld med smalt varmeoverforingsmedium pa sadant satt, att varmeoverforingsmediet i finfOrdelat tillstand medrives av fOrbranningsgaserna genom ejektorverkan da brannaren eller brannarna aro i drift. The invention further relates to an apparatus for carrying out the apparatus, which apparatus can be characterized in that it comprises one or more burners for supplying to the narrow salt mass the heat required for the reaction, which burner or burners are provided with a line for supplying oxygen or oxygen-containing gas and with lines for discharge Dupl. at 10 a: 24/04; 12 g: 1/02; 12 o: 27 of combustion gases, whereby the burner or burners stand. in open connection with a chamber filled with narrow heat transfer medium in such a way that the heat transfer medium in finely divided state is entrained by the combustion gases by ejector action when the burner or burners are in operation.

Uppfinningen lampar sig sarskilt fOr framstallning av olefiner genom krackning av hog-re kolvaten, t. ex. naturgas, raffinaderigas eller mineraloljedestillat sasom nafta eller restoljor. Ett exempel pa en annan reaktion som kan genomforas med hj alp av forfarandet och apparaten enligt uppfinningen är beredningen av vinylklorid genom pyrolys av dikloretan. The invention is particularly suitable for the production of olefins by cracking the higher hydrocarbons, e.g. natural gas, refinery gas or mineral oil distillates such as naphtha or residual oils. An example of another reaction which can be carried out by means of the process and apparatus of the invention is the preparation of vinyl chloride by pyrolysis of dichloroethane.

Temperaturen hos varmeaverfaringsmediet maste givetvis anpassas efter den ifragavarande reaktionen. F8r framstallning av etylen och propylen genom krackning av hogre kolvaten anvandas foretradesvis temperaturer av 800— 1000° C beroende pa arten av utgangsmaterial. The temperature of the heat removal medium must, of course, be adapted to the reaction in question. For the production of ethylene and propylene by cracking the higher hydrocarbons, temperatures of 800-1000 ° C are preferably used, depending on the nature of the starting material.

Sasom varmeoverforingsmedium anvandes foretradesvis ett metallsalt eller en blandning av metallsalter, som under de betingelser vid vilka reaktionen genomfores ha lag flyktighet sâ att inga salter avga fran apparaten tillsammans med reaktionsprodukterna eller fOrbranningsgaserna. Dâ blandningar av salter anvandas aro eutektiska sadana att foredraga. Sarskilt Lampliga salter aro haliderna, foretra, desvis kloriderna, av alkali- och jordalkalimetallerna, sasom natriumklorid, kaliumklorid och bariumklorid, eller motsvarande fluorider och blandningar av dessa salter. Emellertid kunna aven andra metallsalter anvandas, sasom sulfater, sulfider och cyanater. As the heat transfer medium, a metal salt or a mixture of metal salts is preferably used, which under the conditions under which the reaction is carried out has a low volatility so that no salts emit from the apparatus together with the reaction products or the combustion gases. When mixtures of salts are used, eutectic ones are preferred. Particularly suitable salts are the halides, preferably the chlorides, of the alkali and alkaline earth metals, such as sodium chloride, potassium chloride and barium chloride, or the corresponding fluorides and mixtures of these salts. However, other metal salts can also be used, such as sulphates, sulphides and cyanates.

Den vid forfarandet och apparaten enligt 2— — uppfinningen anvanda brannaren bestar i sin enklaste form av ett munstycke, f8rsett med tillforselledningar for bransle och for syre eller syrehaltig gas, samt ett stigr6r som vid den till munstycket anslutna anden har Oppningar for insugning av smalt varmeaverforingsmedium och som Or oppet vid den andra anden. F8retradesvis Or tillforselledningen far branslet anbragt i centrum av munstycket, medan syret eller den syrehaltiga gasen instrommar genom en koaxiell ringformig slits runt bransleinloppet. Stigroret är faretradesvis anbragt koaxiellt med brannarmunstycket. The burner used in the method and apparatus according to the invention consists in its simplest form of a nozzle, provided with supply lines for fuel and for oxygen or oxygen-containing gas, and a riser which has openings for suction of narrow heat transfer medium at the duct connected to the nozzle. and as Or oppet at the other spirit. Preferably, the supply line has the fuel placed in the center of the nozzle, while the oxygen or oxygen-containing gas flows in through a coaxial annular slot around the fuel inlet. The riser is dangerously arranged coaxially with the burner nozzle.

Det Or tydligt att ju langre stigroret fir, des-to Mitre kan varmeoverforingen vara. A andra sidan bar en Overdriven langd hos detta ror undvikas av konstruktiva skal. I allmanhet valjes langden stigroret sa att fOrhallandet mellan langd och diameter ligger mellan 5 och 30. It is clear that the longer the riser fir, the miter the heat transfer can be. On the other hand, an exaggerated length of this rudder should be avoided by constructive shells. In general, the length of the riser is chosen so that the ratio between length and diameter is between 5 and 30.

Stigraret, som faretradesvis placeras i ungefar vertikalt lage med den oppna anden upptill, Or upptill forsett med en anordning far separarering av forbranningsgaserna Iran den medrivna vatskan. Vid en mycket lamplig konstruktion for detta andamal utnyttj as centrifugalkraften av vilken den medrivna vatskan slungas mot en krokt vagg och darigenom separeras Iran forbranningsgaserna. Foretradesvis utmatas forbranningsgaserna i sadan riktning, att de icke passera genom den Atervandande vatskestrommen sa att man undviker att vatskan dispergeras i gasstrommen. The riser, which is dangerously placed in approximately vertical position with the open spirit at the top, Or at the top provided with a device for separating the combustion gases Iran the entrained liquid. In a very suitable construction for this purpose, the centrifugal force is used, from which the entrained liquid is thrown against a crooked rock, and thereby the Iran combustion gases are separated. Preferably, the combustion gases are discharged in such a direction that they do not pass through the regenerating liquid stream so as to avoid dispersing the liquid in the gas stream.

Med den beskrivna konstruktionen av brannaren kan detonerande farbranning eventuellt intraffa i en del fall vid mycket hoga kapaciteter, varvid den smalta massan r8r sig mycket haftigt eller stotvis eller forbranning ager rum utanfor stigraret. En konstruktion vid vilken denna mojlighet undvikes och som dOr- for foredrages far varje brannare bestar av en forkammare med ett eller flera munstycken, vart och ett forsett med tillforselledningar far bransle och syre eller syrehaltig gas, och med ett stigror, som vid ena anden Or anslutet till en appning i namnda kammare och i n5rheten darav har oppningar far insugning av smalt varmeoverforingsmedium samt som Or oppet vid den andra anden. Faretradesvis Oro matarledningarna for branslet anordnade i centrum av munstycket och de for syret eller den syrehaltiga gasen koaxiellt runt bransleledningarna. Brannarmunstyckena Oro foretradevis forsedda med en kylmantel for att forhindra att temperaturen pa materialet blir overdrivet hog. I allmanhet Or diametern hos den oppning i forkammaren, genom vilken forbranningsgaserna kunna avg. till det direkt darmed forbundna stigr8ret, obetydligt mind-re an diametern hos stigroret for att tillfOrsäkra god ejektorverkan och hindra att varmeoverforingsmediet inkommer i f8rkammaren. Stigroret Or foretradesvis koaxiellt med oppningen i f8rkammaren. With the described construction of the burner, detonating color combustion may possibly occur in some cases at very high capacities, whereby the narrow mass moves very violently or in spurts or combustion takes place outside the riser. A construction in which this possibility is avoided and which is therefore preferred for each burner consists of an antechamber with one or more nozzles, each provided with supply lines for fuel and oxygen or oxygen-containing gas, and with a riser, as in one spirit. connected to an opening in the said chamber and in the vicinity thereof there are openings for the suction of narrow heat transfer medium and which are open at the other end. Dangerously concern the supply lines for the fuel arranged in the center of the nozzle and those for the oxygen or oxygen-containing gas coaxially around the fuel lines. The Oro burner nozzles are preferably provided with a cooling jacket to prevent the temperature of the material from becoming excessively high. In general Or the diameter of the opening in the antechamber, through which the combustion gases can escape. to the riser directly connected thereto, insignificantly smaller than the diameter of the riser to ensure good ejector action and to prevent the heat transfer medium from entering the chamber. The riser Or is preferably coaxial with the opening in the antechamber.

Denna konstruktion sakrar inledandet av forbranningen i en zon, i vilken det icke fin- nes nagot varmeaverforingsmedium, och detta leder till stabilitet hos forbranningen. Oppningarna for insugning av vatskeformigt var- meoverforingsmedium befinna sig vid denna konstruktion i stigroret omedelbart ovanfar forkammaren. This construction secures the initiation of combustion in a zone in which there is no heat transfer medium, and this leads to stability of the combustion. The openings for suction of liquid-shaped heat transfer medium are in this construction in the riser immediately above the antechamber.

Pa grund av den intima blandning som sker I stigr8ret Or en preliminar blandning av branslet och syre eller syrehaltig gas icke nodvandig. Due to the intimate mixing that takes place in the riser, a preliminary mixing of the fuel and oxygen or oxygen-containing gas is not necessary.

For att reglera temperaturen och strainningshastigheten hos forbranningsgaserna i stigroret kan en. extra gasstr8m inforas antingen i forkammaren eller i stigroret. Denna gas kan utgaras av luft eller av en inert gas. To regulate the temperature and the straining rate of the combustion gases in the riser, one can. extra gas flow is introduced either into the atrium or into the riser. This gas can be emitted by air or by an inert gas.

Ph grund av den hoga hastigheten has forbranningsgaserna i stigroret insuges det smalta saltet genom oppningarna i stigraret, varigenom den kinetiska energien hos forbranningsgaserna delvis overfores till varmeOver- foringsmediet sO. att en avsevard cirkulation av salt ager rum. Det Or foljaktligen mojligt att undvika den separata regenereringen av den smalta massan genom oxidation av de kolhaltiga fororeningarna. Avlagsnandet av dessa fororeningar ernas genom att till brannaren fora ett ringa overskott av syre eller syrehaltig gas, varigenom fOroreningarna i det med- rivna varmeaverf8ringsmediet i stigr6ret oxideras till kolmonoxid och (om fororeningarna Oven innehalla Tate) vatten. Due to the high speed of the combustion gases in the riser, the narrow salt is sucked in through the openings in the riser, whereby the kinetic energy of the combustion gases is partly transferred to the heat transfer medium sO. that a considerable circulation of salt takes place. It is therefore possible to avoid the separate regeneration of the molten mass by oxidation of the carbonaceous impurities. The removal of these contaminants is effected by feeding to the burner a small excess of oxygen or oxygen-containing gas, whereby the contaminants in the entrained heat transfer medium in the riser are oxidized to carbon monoxide and (if the contaminants also contain Tate) water.

Sasom ett resultat av den hoga cirkulationshastigheten hos det smalta varmeoverforings- mediet genom brannaren Or genomsnittliga tidsperioden mellan varmeoverforingen i reaktorn och regenereringen i brannaren helt kort och foljaktligen oxideras de kolhaltiga Wore- ningarna innan de kunna giva upphov till bildandet av grafit. Det har visat sig, att sh.dan grafit Or mycket svar att avlagsna genom oxidation och dad& kan medfora en permanent fororening av varmeoverforingsmediet. As a result of the high circulation speed of the narrow heat transfer medium through the burner, the average time period between the heat transfer in the reactor and the regeneration in the burner is very short and consequently the carbonaceous warnings are oxidized before they can give rise to graphite formation. It has been found that sh.dan graphite Or much response to precipitation by oxidation and dad & can cause a permanent contamination of the heat transfer medium.

Uppfinningen fartydligas i det foljande med hanvisning till bifogade ritning. — Fig. 1 visar en. vertikalsektion genom en apparat med rektangular tvarsektion, i vilken det finnes en r8rformig reaktor i centrum och tva brannare placerade p0 var sin sida om reaktorn. — Fig. 2 visar en vertikalsektion genom en rorformig reaktor. — Fig. 3 visar en langdsektion genom en brannare. — Fig. 4 visar i storre skala och i sektion en del av en brannare forsedd med en forkammare. The invention is explained in the following with reference to the accompanying drawing. Fig. 1 shows a. vertical section through an apparatus with a rectangular cross-section, in which there is a tubular reactor in the center and two burners placed on each side of the reactor. Fig. 2 shows a vertical section through a tubular reactor. Fig. 3 shows a longitudinal section through a burner. Fig. 4 shows on a larger scale and in section a part of a burner provided with an antechamber.

Apparaten Or uppbyggd av en stalmantel 1, som har ett foder av varmeisolerande tegel 2. The apparatus Or is made up of a steel jacket 1, which has a lining of heat-insulating bricks 2.

Rummet 3 innehallande varmeoverforingsme- diet omgives av ett skikt av tegel 4 som mot-star bade den hoga temperaturen hos detta medium och dess kemiska inverkan. I detta rum Or anordnad en rorformig reaktor 5 och tva. brannare 6. Dessa kunna besta av ror av exempelvis keramiskt material. Alternativt - - kunna de utgaras av kanaler kvarlamnade i tegelskiktet 4. The room 3 containing the heat transfer medium is surrounded by a layer of brick 4 which resists both the high temperature of this medium and its chemical effect. In this room Or arranged a tubular reactor 5 and two. burners 6. These can consist of pipes of, for example, ceramic material. Alternatively - - they can be made of channels left in the brick layer 4.

Matningen av utgangsmaterial till den Darformiga reaktorn 5 sker genom ett munstycke 7 och materialet strommar uppat med hog hastighet. Varmeoverforingsmediet suges samtidigt in genom oppningar 8 och dispergeras i den uppatstigande materialstrammen. Vid Ovre anden av reaktorn separeras varmeaverf8- ringsmediet fran produkten i en separator 9 och strommar genom en kanal 10 tillbaka till kammaren 3. Produkten utmatas genom ledningar 11. The feed material to the Dar-shaped reactor 5 takes place through a nozzle 7 and the material flows upwards at high speed. The heat transfer medium is simultaneously sucked in through openings 8 and dispersed in the ascending material stream. At the upper end of the reactor, the heat transfer medium is separated from the product in a separator 9 and flows through a channel 10 back to the chamber 3. The product is discharged through lines 11.

Bransle och syre eller syrehaltig gas inf5ras genom munstycken 12 i brannarna. Genom Oppningar 13 insuges varmeaverforingsmedium och dispergeras i de genom ett stigror 14 strOmmande forbranningsgaserna. Efter separation frail forbranningsgaserna strommar varmeoverforingsmediet tillbaka till kammaren 3 och farbranningsgaserna avga genom leclningar 15. Fuel and oxygen or oxygen-containing gas are introduced through nozzles 12 into the burners. Heat transfer medium is sucked through openings 13 and dispersed in the combustion gases flowing through a riser 14. After separation from the combustion gases, the heat transfer medium flows back to the chamber 3 and the combustion gases emit through leaks 15.

Far separering av varmeaverfOringsmediet frdn forbranningsgaserna finnes en. separator 9a ovanf5r stigroret till brannaren. I denna avb5jes gasstrommen av vaggar 18 som dro krata vasentligen i en riktning. Till foljd av den ddrigenom upptradande centrifugalkraften slungas dropparna mot dessa vaggar och matas i form av en vatskefilm i riktning nedlfings dessa vaggar. Farbranningsgaserna avga i en riktning som är parallell med de krokta vaggarnas periferier utan att komma I begging med de separerade dropparna. Separatorn 9 °yangr den rorformiga reaktorn Sr av samma konstruktion som separatorn 9a ovanfor brannarna. If the heat transfer medium is separated from the combustion gases, there is one. separator 9a above the riser to the burner. In this, the gas stream is deflected by rocks 18 which pulled the crater substantially in one direction. As a result of the centrifugal force thus occurring, the droplets are thrown towards these rocks and fed in the form of a liquid film in the direction of these rocks. The combustion gases emit in a direction parallel to the peripheries of the curved rocks without coming into contact with the separated droplets. The separator 9 ° is the tubular reactor Sr of the same construction as the separator 9a above the burners.

Den i fig. 4 visade brannaren har en forkammare 16, i vilken forbranningen inledes. The burner shown in Fig. 4 has an antechamber 16, in which the combustion is initiated.

Forkammaren är ansluten till stigrOret 14 genom en oppning 17. Oppningarna 13 for varmeoverforingsmediet aro anordnade ovanfOr forkammaren. The antechamber is connected to the riser 14 through an opening 17. The openings 13 for the heat transfer medium are arranged above the antechamber.

Exempel. Foljande exempel är baserat pa ett Virg& utfort i en apparat av den ovan be- skrivna typen. De hada brannarna voro for- sedda med en forkammare med en ldngd av 25 cm och en diameter av 6 cm. Stigroret hade en ldngd av 120 cm och en diameter av 6,5 cm. Example. The following example is based on a Virg & performed in an apparatus of the type described above. The hot fires were equipped with an antechamber with a length of 25 cm and a diameter of 6 cm. The riser had a length of 120 cm and a diameter of 6.5 cm.

Denna apparat anvandes for framstallning av eten och propen med utgang fran propan. This apparatus is used for the production of ethylene and propylene starting from propane.

For andamalet satsades i apparaten 690 kg av en blandning av 80 % bariumklorid och 20 % natriumklorid, vilken blandning h5lls vid en temperatur av 900° C genom forbranning av propan i tva. brannare. Vid en matningshastighet av 8 kg propan per tiname till var och en av brannarna erhalls en varmealstring av 5,6 X 7 kcal/ms, varav 63 % averfordes till salterna. For this purpose, 690 kg of a mixture of 80% barium chloride and 20% sodium chloride were charged into the apparatus, which mixture was kept at a temperature of 900 ° C by burning propane in two. burner. At a feed rate of 8 kg of propane per tiname to each of the burners, a heat generation of 5.6 X 7 kcal / ms was obtained, of which 63% was transferred to the salts.

Propan inmatades i reaktorn i en mangd. av 75 kg/h. Den resulterande produkten hade f51- jande sarnmansattning: Vol. % Vikts 0/0 112 16,9 1, CH4 31,4 22,3 C2114 30,4 37,8 C2H 6 4,7 6,3 C3116 6,1 11,3 C31-18 9,6 18,6 C4H6 0,9 2,2 Air utgangsmaterialet omvandlades mindre an 1 % till kolhaltiga fororeningar, vilka avlagsnades ur varmeaverforingsmediet under regenereringen. 49,1 % av utgangsmaterialet omvandlades till eten och propen. Propane was fed into the reactor in an amount. of 75 kg / h. The resulting product had the following composition: Vol. % Weight 0/0 112 16.9 1, CH4 31.4 22.3 C2114 30.4 37.8 C2H 6 4.7 6.3 C3116 6.1 11.3 C31-18 9.6 18.6 C4H6 The 0.9 2.2 Air starting material was converted less than 1% to carbonaceous impurities, which were removed from the heat transfer medium during the regeneration. 49.1% of the starting material was converted to ethylene and propylene.

Exempel 2. Samma apparat som i exempel 1 anvandes for krackning av bensin till en gasblandning av innehallande eten och propen. Utgangsmaterialet utgjordes av en bensin med ett kokpunktsomrade av 40-100° C. Ternperaturen hos varmeaverforingsmediet (en blandning av BaC12 och NaC1) halls vid 850° C genom forbranning av propan sasom i foregaende exempel. Example 2. The same apparatus as in Example 1 was used for cracking gasoline into a gas mixture of ethylene and propylene. The starting material was a gasoline having a boiling point range of 40-100 ° C. The temperature of the heat transfer medium (a mixture of BaCl 2 and NaCl) was maintained at 850 ° C by combustion of propane as in the previous example.

Vid en avverkning av 100 kg bensin per timme erh011s en produkt av foljande sammansattning: Vol. % Vikts % 112 14,6 1,1 CH4 29,6 18,3 C2H4 31,0 33, C2116 3,2 3,7 C3116 10,3 16,7 C3H8 2,0 3,4 hogre kolvaten 9,3 23,3 Air utgangsmaterialet omvandlades mindre an 1 % till kolhaltiga fororeningar som avlagsnades ur varmeoverf5ringsmediet under regenereringen. 50,2 % av utgangsmaterialet omvandlades till eten och propen. At a felling of 100 kg of petrol per hour, a product of the following composition is obtained: Vol. % Weight% 112 14.6 1.1 CH4 29.6 18.3 C2H4 31.0 33, C2116 3.2 3.7 C3116 10.3 16.7 C3H8 2.0 3.4 higher hydrocarbons 9.3 23 The Air starting material was converted less than 1% to carbonaceous impurities which were removed from the heat transfer medium during the regeneration. 50.2% of the starting material was converted to ethylene and propylene.

Claims

Patent claim:

1. Set according to claim 3 of patent 178 150 for the production of normally gaseous olefins, characterized in that the heating of the salt in the regeneration zone takes place by supplying heat from combustion of a liquid or gaseous fuel in a burner, the narrow salt mass being taken off by the combustion gases in finely divided state by ejector action and then lean these gases are separated.

Apparatus for carrying out the kit according to claim 1, characterized in that it comprises one or more burners (6) for supplying to the narrow salt mass the heat required for the reaction, which burner or burners are connected by line (12). f Sr supply of oxygen or oxygen-containing gas saint with lines (15) for the discharge of combustion gases, the burner or fire.- - - llama standing in open communication with a chamber (3) filled with narrow salt in such a way that salts in finely divided condition is entrained by the combustion gases by ejector action when the burner or burners are in operation.

Apparatus according to claim 2, characterized in that the burner or burners (6) existed. of a nozzle (12) provided with supply lines for fuel and for oxygen or oxygen-containing gas and a riser (14), which at the duct connected to the nozzle has openings (13) for suction of narrow salt and which is open at the other duct.

Apparatus according to patent claim 3, Milne-signed, that the supply line for the fuel is arranged in the center of the nozzle (12) and that the supply line for oxygen or oxygen-containing gas is arranged coaxially around the supply line for fuel.

Apparatus according to claim 3 or 4, characterized in that the riser (14) is arranged coaxially with the nozzle.

Apparatus according to claim 2, characterized in that the burner or burners (6) consist. of an antechamber (16) with one or more nozzles, each of which is provided with supply lines for fuel and for oxygen or oxygen-containing gas, and a riser (14), which at one end Si is connected to an opening (16) in The rear chamber and in the vicinity thereof have openings (13) for sucking in narrow salt and which is the tip at the other end.

7. Apparatus according to claim 6, characterized in that the supply line or lines for the fuel are arranged in one room of the burner nozzle or nozzles (12) and that the supply line or lines for oxygen or oxygen-containing gas are arranged coaxially around the fuel supply line or lines. .

8. Apparatus according to claim 6 or 7, characterized in that the riser (14) is arranged coaxially with the opening. (17) in the antechamber.

Apparatus according to any one of claims 3 to 8, characterized in that the ratio between the length and diameter of the riser (14) amounts to between 5 and 30.

10. Apparatus according to any one of claims 3-9, characterized in that it. Equipped with lines for supplying air or gas to the riser (14) or the antechamber (16) for regulating the temperature and / or the rate of combustion of the combustion gases in the riser. Request publications: