DE102005048488C5 - Method and device for high power entrained flow gasifiers - Google Patents

Abstract

Device for carrying out a method according to claims 13 to 21 for the gasification of fuel dust-water slurry or fuel dust-oil slurry or solid fuels in flight flow with a free oxygen-containing oxidizing agent by partial oxidation at pressures between ambient pressure and 8 MPa, temperatures between 1,200 and 1,900 ° C and high reactor outputs in which a high-performance gasification reactor (2) has a plurality of gasification burners (2.1) arranged at the head and an ignition and pilot burner (2.2), characterized in that each gasification burner (2.1) is assigned its own fuel supply system - there is an arrangement on the gasification burner (2.1) for measuring and regulating the amount of fuel and oxygen flowing in and - there is an integral monitoring and control of the amount of fuel and oxygen flowing in total to the gasification reactor (2).

Description

The invention relates to a device and a method for entrained-flow gasification of very high power, as can be used for supplying synthesis gas to large-scale syntheses. The invention allows fuels such as lignite and hard coal, petroleum coke, solid milled residues but also solid-liquid suspensions, so-called slurries, to be converted into synthesis gas. The fuel is converted at temperatures between 1,200 and 1,900 ° C with a free oxygen-containing gasifying agent at pressures up to 8 MPa by partial oxidation into gases containing CO and H ₂ . This takes place in a gasification reactor, which is characterized by a multi-burner arrangement and by a cooled gasification chamber.

The autothermal entrained-flow gasification of solid, liquid and gaseous fuels has long been known in the art of gas generation. The ratio of fuel to oxygen-containing gasification agents is chosen so that, for reasons of synthesis gas quality, higher carbon compounds to synthesis gas components such as CO and H2 are completely broken down and the inorganic constituents are discharged as molten slag, see J. Carl, P. Fritz, NOELL CONVERSION PROCESS , EF-Verlag für Energie- und Umwelttechnik GmbH, 1996, p. 33 and p. 73.

According to various systems introduced in technology, gasification gas and molten slag can be separated or discharged together from the reaction space of the gasification device, such as DE 197 18 131 A1 shows. For the internal limitation of the reaction space structure of the gasification system, both systems provided with a refractory lining or cooled systems have been introduced, see DE 4446 803 A1 .

EP 0677 567 B1 and WO 96/17904 show a method in which the gasification space is limited by a refractory lining. This has the disadvantage that the refractory masonry is detached by the liquid slag formed during the gasification, which leads to rapid wear and tear and high repair costs. This wear process increases as the ash content increases. Such gasification systems therefore have a limited runtime until the lining is renewed. In addition, the gasification temperature and the ash content of the fuel are limited. The supply of the fuel as a coal-water slurry brings considerable losses in efficiency, see C. Higman u. M. van der Burgt, “Gasification”, Verlag ELSEVIER, USA, 2003, which can be reduced or avoided by using oil as a carrier medium or by preheating the coal-water slurry. The simplicity of the feed system is advantageous. Furthermore, a quench or cooling system is described, in which the hot gasification gas and the liquid slag are discharged together via a guide tube, which begins at the lower end of the reaction space, and passed into a water bath. This joint discharge of gasification gas and slag can lead to blockage of the guide tube and thus to the limitation of availability.

DE 3534015 A1 shows a method in which the gasification media fine coal and oxygen-containing oxidizing agent are introduced into the reaction chamber via several burners in such a way that the flames deflect each other. The gasification gas flows fine dust laden upwards and the slag downwards into a slag cooling system. As a rule, a device for indirect cooling using the waste heat is provided above the gasification chamber. However, entrained liquid slag particles pose a risk of the heat exchanger surfaces being deposited and covered, which leads to obstruction of the heat transfer and possibly to a blockage of the pipe system or to erosion. The risk of constipation is counteracted by removing the hot raw gas with a circulating cooling gas.

In Ch. Higman and M. van der Burgt, in “Gasification”, page 124, Elsevier Publishing House 2003, a process is presented in which the hot gasification gas, together with the liquid slag, leaves the gasifier and enters directly into a waste heat boiler arranged vertically below which the raw gas and the slag using the

Waste heat can be cooled to generate steam. The slag collects in a water bath, the cooled raw gas leaves the waste heat boiler sideways. The advantage of waste heat recovery according to this system is offset by a number of disadvantages. The formation of deposits on the heat exchanger tubes, which lead to the obstruction of heat transfer as well as to corrosion and erosion and thus to a lack of availability, should be mentioned here in particular.

CN 2700718 Y describes a “solid powdered fuel gasifier”, in which the coal dust is fed pneumatically and gasification gas and liquefied slag are introduced into a water bath via a central pipe for further cooling. This central drainage in the central pipe mentioned is susceptible to blockages which disrupt the overall operation and reduce the availability of the entire system.

The performance of the various gasification technologies presented is limited to approx. 500 MW.

Based on this prior art, it is an object of the invention to provide a device for the gasification of fuel dust-water slurry or fuel dust-oil slurry solid fuels in the entrained flow, and a method for carrying out this device, which operate in a reliable and safe manner allow maximum outputs from 1,000 to 1,500 MW.

This object is achieved by a device for the gasification of fuel dust-water slurry or fuel dust-oil slurry solid fuels in the entrained flow according to claim 1 and a method for carrying out this device according to claim 13. Subclaims represent advantageous embodiments of the invention.

The invention makes use of the knowledge that the fuel supply to the gasification reactor forms a bottleneck for the performance of the gasification reactor.

The gasification process for the gasification of solid ash-containing fuels at very high outputs with an oxygen-containing oxidizing agent is based on an entrained-flow reactor whose reaction space contour is limited by a cooling system, the pressure in the cooling system always being kept higher than the pressure in the reaction space. For the preparation of the fuel and the supply to the gasification burners, the procedure is as follows: In the case of a dry pneumatic supply based on the principle of dense phase conveyance, the fuel is dried, crushed to a grain size of <200 µm and pressure locks are fed into the operating bunker, in which a non-condensing feed is supplied Gas such as N2 or CO2 the dusty fuel is brought to the desired gasification pressure. Different fuels can be used at the same time. By arranging several of these pressure locks, filling and pressure can be applied alternately. The pressurized dust then enters metering vessels in which a very dense fluidized bed is created in the lower part by supplying a non-condensing gas as well, into which one or more delivery tubes are immersed and which open into the burners of the gasification reactor. Each high-performance burner is assigned a separate feed and metering system. By applying a pressure difference between the metering vessels and the burners of the gasification reactor, the fluidized fuel dust flows to the burners. The flowing amount of fuel dust is measured, regulated and monitored by measuring and monitoring devices.

With the proposed reactor there is still the possibility of also comminuting the undried fuel to a grain size of <200 μm and mixing the fuel dust with water or oil and supplying it to the burners of the gasification reactor as a slurry. The person skilled in the art designs the method for feeding, which is not described here, using the means known to him.

An oxidizing agent containing free oxygen is simultaneously fed to the burners and the slurry is converted into a raw synthesis gas by partial oxidation. Gasification takes place at temperatures between 1,200 and 1,900 ° C at pressures up to 80 bar. The reactor has a cooled reaction space contour, which is formed by a cooling screen. This consists of a gas-tight welded tubular screen, which is pinned and covered with a highly temperature-conductive material.

The raw gas generated in the gasification reactor leaves the gasification reactor together with the liquid slag formed from the fuel ash and arrives in a space arranged vertically below, in which the hot raw gas and the liquid slag are cooled by injecting water. The cooling can take place completely up to the dew point of the gas by injecting excess water. Depending on the pressure, the temperature is then between 180 and 240 ° C. However, it is also possible to supply only a limited amount of cooling water and to cool the raw gas and slag by partial cooling to, for example, 700 to 1,100 ° C. in order to then use the sensible heat of the raw gas in a waste heat boiler to generate steam. The partial quenching or partial cooling prevents or severely limits the risk of slag caking on the pipes of the waste heat boiler. The water or recirculated gas condensate required for complete or partial cooling is supplied via nozzles that are located directly on the jacket of the cooling room. The cooled slag is collected in a water bath and removed from the process. The raw gas cooled to temperatures between 200 and 300 ° C. then passes into a raw gas scrubber, which is expediently designed as a venturi scrubber.

The dust that is carried along is removed up to a grain size of approx. 20 µm. This degree of purity is not yet sufficient to subsequently carry out catalytic processes such as raw gas conversion. It should also be borne in mind that salt mist is also carried in the raw gas, which is released from the fuel dust during the gasification and removed with the raw gas. To remove both the fine dust <20 µm and the salt spray washed raw gas is fed to a condensation stage in which the raw gas is indirectly cooled by 5 to 10 ° C. Water is condensed from the water vapor-saturated raw gas and absorbs the fine dust and salt particles described. In a subsequent separator, the condensed water containing the dust and salt particles is removed from the raw gas. The raw gas purified in this way can then be fed directly, for example, to a desulfurization plant.

• 1: Blockschema der Technologie
• 2: Dosiersystem für Brennstaub
• 3: Vorrichtung der Brennstaubzuführung für Hochleistungsgeneratoren
• 4: Vergasungsreaktor mit Vollquenchung
• 5: Vergasungsreaktor mit Teilquenchung

The invention is explained in more detail below with the aid of 5 figures and two exemplary embodiments. The figures show:

• 1 : Block diagram of the technology
• 2nd : Dosing system for fuel dust
• 3rd : Device for supplying fuel dust for high-performance generators
• 4th : Gasification reactor with full quenching
• 5 : Gasification reactor with partial quenching

The 1 shows in a block diagram the process steps of pneumatic dosing of fuel dust, gasification in a gasification reactor with a cooled reaction chamber structure 2nd , Quench cooling 3rd , Raw gas scrubbing 4th , being between the quench cooling 3rd and raw gas scrubbing 4th a waste heat boiler 4.1 can be arranged and the raw gas scrubbing 4th a condensation or partial condensation 5 follows.

The 2nd shows a dosing system for fuel dust, consisting of a bunker 1.1 , the two pressure locks 1.2 are connected downstream in the lines 1.6 lead for inert gas and in the upper part expansion lines 1.7 lead out, taking the pressure locks 1.2 down lines to the dosing vessel 1.3 leave. At the pressure locks 1.2 fittings for monitoring and control are arranged. A line leads from below into the dosing vessel 1.5 for fluidizing gas, which ensures that the fuel is fluidized and via the delivery line 1.4 the fluidized fuel dust in a gasification reactor 2nd is fed.

The 3rd shows another embodiment of the device for supplying fuel dust for high-performance generators 2nd being a bunker 1.1 with three outlets for fuel dust to pressure locks 1.2 leads, with three pressure locks of fuel dust flows to three dosing vessels 1.3 promote, of which conveyor lines 1.3 to the dust burners 1.2 lead with oxygen supply to the reactor. At the reactor 2nd are three dust burners each 2.1 arranged with oxygen supply, with a pilot and pilot burner 2.2 is there to start the reaction. With such intensive fluidized fuel flows and the presence of three burners 2.1 it is possible to achieve maximum outputs of 1,000 to 1,500 megawatts with reliable and safe operation.

The 4th shows a gasification reactor 2nd with full quenching 3rd , being in the head of the reactor 2nd in the middle the pilot and pilot burner 2.2 and the dust burner 2.1 are arranged through which fluidizing gas or a mash of fuel and liquid are fed into the reactor. The reactor has a gasification room 2.3 with a cooling screen 2.4 on whose outlet opening 2.5 to the quench cooler 3rd leads, its quench room 3.1 Quench nozzles 3.2 , 3.3 has and a raw gas outlet 3.4 through which the finished raw gas passes the quench cooler 3rd can leave. At the bottom of the quench cooler is in a water bath 3.5 the slag is cooled by an outlet 3.6 leaves the quench cooler.

The 5 shows a gasification reactor 2nd with partial quenching, with the gasification reactor arranged in the upper part, in the dust burner 2.1 the dust from the delivery line 1.4 gasify and a pilot and pilot burner in the middle 2.2 is arranged. The gasification reactor 2nd has an opening down into the quench chamber 3.1 on, in the quench nozzles on both sides 3.2 lead, below this heat recovery boiler 4.1 are arranged.

• Einem Vergasungsreaktor mit einer Bruttoleistung von 1500 MW wird eine Kohlenstaubmenge von 240 Mg/h zugeführt. Dieser durch Trocknung und Mahlung aus Rohsteinkohle hergestellte Brennstaub besitzt einen Feuchtigkeitsgehalt von 5,8%, einen Aschegehalt von 13 Ma% und einen Heizwert von 24.700 kJ/kg. Die Vergasung findet bei 1.550°C statt, die benötigte Sauerstoffmenge beträgt 208.000 m³ i. N./h. Die Rohkohle wird zunächst einer dem Stand der Technik entsprechende Trocknungs- und Mahlanlage zugeführt, in der der Wassergehalt auf 1,8 Ma% reduziert wird. Das nach der Mahlung vorhandene Körnungsband des aus der Rohkohle hergestellten Brennstaubes liegt zwischen 0 und 200 µm. Danach wird der gemahlene Brennstaub (1) dem Dosiersystem zugeführt, dessen Funktionsprinzip in 2 gezeigt ist. Das Dosiersystem besteht aus drei gleichen Einheiten wie das 3 zeigt, wobei jede Einheit 1/3 der Gesamtstaubmenge, also 80 Mg/h, je einem Staubbrenner zuführt. Die drei dazugehörigen Staubbrenner befinden sich am Kopf des Vergasungsreaktors, dessen Prinzip 4 zeigt. Der einsatzfähige Brennstaub gelangt nach 2. die eine Einheit des Staubdosiersystems zeigt, aus dem Betriebsbunker 1.1 in wechselseitig betriebene Druckschleusen 1.2. In jeder Einheit sind 3 Druckschleusen angeordnet. Die Aufpufferung auf den Vergasungsdruck geschieht mit einem inerten Gas wie beispielsweise Stickstoff, der über die Leitung 1.6 zugeführt wird. Nach der Aufpufferung wird der unter Druck stehende Brennstaub dem Dosiergefäß 1.3 zugeführt. Die Druckschleusen 1.2 werden über die Leitung 1.7 entspannt und können erneut mit Brennstaub befüllt werden. Die 3 genannten Druckschleusen in jeder Einheit werden wechselseitig befüllt, bespannt, in das Dosiergefäß entleert und entspannt. Danach beginnt dieser Vorgang erneut. Durch Zuführung eines als Fördergas dienenden trockenen Inertgases, beispielsweise gleichfalls Stickstoff über die Leitung 1.5 wird im Unterteil des Dosiergefäßes 1.3 eine dichte Wirbelschicht erzeugt, in die 3 Staubförderleitungen 1.4 hineinragen. Die in den Förderleitungen 1.4 fließende Brennstaubmenge wird überwacht, gemessen und in Relation zum Vergasungssauerstoff geregelt. Der Vergasungsreaktor 2 ist in 3 gezeigt und näher erläutert. Die Förderdichte beträgt 250-420 kg/m³. Der Vergasungsreaktor 2 ist in 3 gezeigt und näher erläutert. Der über die Förderleitungen 1.4 dem Vergasungsreaktor 2 zufließende Brennstaub wird (3) in 3 Dosiersysteme mit einer Kapazität von je 80 Mg/h geschleust. Die insgesamt 9 Förderleitungen 1.4 führen jeweils in Dreiergruppen zu 3 am Kopf des Reaktors 2 angeordneten Vergasungsbrennern 4.1. Gleichzeitig werden jedem Vergasungsbrenner 1/3 der Gesamtsauerstoffmenge von 208.000 Nm³/h zugeführt. Die Staubbrenner sind symmetrisch im Winkel von 120° angeordnet, im Zentrum befindet sich ein Zünd- und Pilotbrenner, der dem Aufheizen des Vergasungsreaktors 2 und der Zündung des Staubbrenners 4.1 dient. Im Vergasungsraum 2.3, der sich durch eine gekühlte Reaktionsraumkontur 2.4 auszeichnet, findet die Vergasungsreaktion, also die partielle Oxidation bei Temperaturen von 1.550°C statt. Die überwachten und gemessenen Brennstaubmengen werden einer Verhältnisregelung mit dem zugeführten Sauerstoffe unterzogen, die dafür sorgt, dass das Verhältnis von Sauerstoff zu Brennstoff einen Bereich von λ = 0,35 bis 0,65 nicht unter- oder überschreitet. Der λ-Wert stellt dabei das Verhältnis der benötigten Sauerstoffmenge bei der gewünschten Partialoxidation zu der Sauerstoffmenge dar, die bei vollständiger Verbrennung des eingesetzten Brennstoffes erforderlich wäre. Die entstandene Rohgasmenge beträgt 463 000 Nm³/h und zeichnet sich durch folgende Analyse aus:

H₂ 19,8 Vol.% CO 70,3 Vol.% CO₂ 5,8 Vol.% N₂ 3,8 Vol.% NH₃ 0,03 Vol.% HCN 0,003 Vol.% COS 0,04 Vol.% H₂S 0,4 Vol.% Using a first example, the function should be explained using material flows and process engineering processes:

• A coal dust quantity of 240 mg / h is fed to a gasification reactor with a gross output of 1500 MW. This fuel is made from raw coal by drying and grinding and has a moisture content of 5.8%, an ash content of 13% and a calorific value of 24,700 kJ / kg. The gasification takes place at 1,550 ° C, the amount of oxygen required is 208,000 m ³ i. N./h. The raw coal is first fed to a drying and grinding plant corresponding to the state of the art, in which the water content is reduced to 1.8% by mass. The grain size range of the fuel dust produced from the raw coal after grinding is between 0 and 200 µm. Then the ground fuel dust ( 1 ) fed to the dosing system, the principle of which is described in 2nd is shown. The dosing system consists of three identical units as that 3rd shows, each unit 1 / 3rd the total amount of dust, i.e. 80 mg / h, is fed to a dust burner. The three associated dust burners are located on the head of the gasification reactor, its principle 4th shows. The usable fuel dust arrives 2nd . which shows a unit of the dust dosing system, from the operating bunker 1.1 in mutually operated pressure locks 1.2 . 3 pressure locks are arranged in each unit. Buffering to the gasification pressure takes place with an inert gas such as nitrogen, which is supplied via the line 1.6 is fed. After the buffering, the fuel dust under pressure is transferred to the dosing vessel 1.3 fed. The pressure locks 1.2 be over the line 1.7 relaxed and can be refilled with fuel dust. The 3rd Pressure locks in each unit are alternately filled, covered, emptied into the metering vessel and relaxed. Then this process starts again. By supplying a dry inert gas which serves as the conveying gas, for example likewise nitrogen, via the line 1.5 is in the lower part of the dosing vessel 1.3 creates a dense fluidized bed in the 3 dust conveyor lines 1.4 protrude. The in the delivery lines 1.4 Flowing amount of fuel dust is monitored, measured and regulated in relation to the gasification oxygen. The gasification reactor 2nd is in 3rd shown and explained in more detail. The delivery density is 250-420 kg / m ³ . The gasification reactor 2nd is in 3rd shown and explained in more detail. The over the delivery lines 1.4 the gasification reactor 2nd incoming fuel dust is ( 3rd ) in 3 dosing systems with a capacity of 80 mg / h each. The total of 9 delivery lines 1.4 lead in groups of three to 3 at the top of the reactor 2nd arranged gasification burners 4.1 . At the same time, every gasification burner 1 / 3rd the total amount of oxygen of 208,000 Nm ³ / h supplied. The dust burners are arranged symmetrically at an angle of 120 °, in the center there is an ignition and pilot burner, which is used to heat the gasification reactor 2nd and the ignition of the dust burner 4.1 serves. In the gasification room 2.3 , which is characterized by a cooled reaction chamber contour 2.4 distinguished, the gasification reaction, i.e. the partial oxidation takes place at temperatures of 1,550 ° C. The monitored and measured amounts of fuel dust are subjected to a ratio control with the supplied oxygen, which ensures that the ratio of oxygen to fuel does not fall below or exceed a range of λ = 0.35 to 0.65. The λ value represents the ratio of the amount of oxygen required for the desired partial oxidation to the amount of oxygen that would be required if the fuel used were completely combusted. The resulting raw gas volume is 463,000 Nm ³ / h and is characterized by the following analysis:

H ₂ 19.8% by volume CO 70.3 vol.% CO ₂ 5.8 vol.% N ₂ 3.8 vol.% NH ₃ 0.03 vol.% HCN 0.003 vol.% COS 0.04 vol.% H ₂ S 0.4 vol.%

The 1 .550 ° C hot raw gas leaves the gasification chamber together with the liquid slag 2.3 about expiry 2.5 and is in the quench room 3.1 by injecting water through the rows of nozzles 3.2 and 3.3 Chilled to 212 ° C and reaches the outlet 3.4 in the raw gas wash 4th that serves as a water wash to remove dust. The cooled slag collects in a water bath 3.5 and is discharged downwards. The water-washed raw gas arrives after the water wash 4th into a partial condensation 5 to fine dust <20 µm as well as in water washing 4th to remove salt mist that has not separated. For this purpose, the raw gas is cooled by approx. 5 ° C, whereby the salt particles dissolve in the condensed water droplets. The cleaned, water vapor-saturated raw gas can then be fed directly to a catalytic raw gas conversion or other treatment stages.

According to an example 2, the process of supplying fuel dust is said to follow 2nd and 3rd and the actual gasification are the same as in Example 1. The hot raw gas and the hot liquid slag are discharged 2.5 also in a quench room 3.1 , in which not with excess water but only by injecting a limited amount of water through nozzle rings 3.2 The raw gas is cooled to temperatures of 700-1,100 ° C and then in the waste heat boiler 4.1 use the sensible heat of the raw gas to generate steam, ( 5 ). The temperature of the partially cooled raw gas is selected so that the slag particles carried have cooled down in order to avoid deposits on the heat exchanger tubes. As in Example 1, the raw gas cooled to approx. 200 ° C is then fed to the water wash and partial condensation.

Reference list

1

Pneumatic dosing systems for fuel dust

1.1

bunker

1.2

Pressure lock

1.3

Dosing vessel

1.4

Conveyor line

1.5

Line for fluidizing gas

1.6

Line for inert gas in 1.2

1.7

Relaxation line 1.2

2nd

Gasification reactor with a cooled reaction chamber structure

2.1

Dust burner with oxygen supply

2.2

Pilot and pilot burner

2.3

Gasification room

2.4

Cooling screen

2.5

Outlet opening

3rd

Quench cooler

3.1

Quench room

3.2

Quench nozzles

3.3

Quench nozzles

3.4

Raw gas outlet

3.5

Water bath with slag

3.6

Lower exit from 3rd

3.7

lining

4th

Raw gas scrubbing

4.1

Waste heat boiler

5

Condensation, partial condensation

Claims (21)

Device for carrying out a method according to the Claims 13 to 21 for the gasification of fuel dust-water slurry or fuel dust-oil slurry or solid fuels in the entrained flow with a free oxygen-containing oxidizing agent by partial oxidation at pressures between ambient pressure and 8 MPa, temperatures between 1,200 and 1,900 ° C and high reactor outputs at the - High-performance gasification reactor (2) has a plurality of gasification burners (2.1) arranged at the head and an ignition and pilot burner (2.2), characterized in that - each gasification burner (2.1) is assigned its own fuel supply system, - an arrangement on the gasification burner (2.1) for Measuring and regulating the inflowing fuel and oxygen quantities is given and - an integral monitoring and regulation of the total inflowing fuel and oxygen quantity is given to the gasification reactor (2). Device after Claim 1 characterized in that fuel gas can be fed to a gasification burner (2.1) via a plurality of delivery lines (1.4) from an individually assigned metering vessel (1.3). Device after Claim 2 characterized in that a metering vessel (1.3) can be fed with fuel dust through a plurality of individually assigned pressure locks (1.2). Device according to one of the preceding Claims 2 to 3rd characterized in that the pressure locks (1.2) can be fed with fuel dust from a bunker common to a plurality of gasification burners. Device according to one of the preceding claims, characterized in that the gasification reactor has three gasification burners (2.1) arranged symmetrically at the head. Device according to one of the preceding Claims 2 to 5 characterized in that a gasification burner (2.1) is connected to its metering vessel (1.3) via three delivery lines (1.4). Device according to one of the preceding Claims 2 to 6 characterized in that a metering vessel (1.3) is connected to three assigned pressure locks (1.2). Device according to one of the preceding Claims 2 to 7 characterized in that a quench chamber (3) for cooling the raw gas generated in the gasification reactor (2) and the slag is arranged. Device after Claim 8 characterized in that the quench chamber (3) is followed by a combination with a raw gas scrubber (4) and a cooler (5) for carrying out a partial condensation. Device according to one of the preceding Claims 2 to 7 characterized in that a quench chamber (3) for the partial cooling of the raw gas generated in the gasification reactor (2) and the slag with a subsequent combination with a waste heat boiler for the production of steam are arranged with further cooling of the raw gas and slag as well as a subsequent water washing and partial condensation. Device according to one of the preceding Claims 2 to 6 characterized in that the gasification reactor (2) is followed by partial cooling to temperatures between 700-1,100 ° C and heat recovery by steam generation from the sensible heat of the raw gas. Device according to one of the preceding claims, characterized in that the gasification reactor has a cooled reaction space contour. Gasification process for implementation in a device according to one of the preceding Claims 1 to 12th , consequently - gasification of fuels, especially solid fuels such as hard coal, lignite and their coke, petroleum coke, coke made of peat or biomass, in flight flow with an oxidizing agent containing free oxygen by partial oxidation at pressures between ambient pressure and 8 MPa and temperatures between 1,200 and 1,900 ° C is carried out at high reactor outputs between 1,000 and 1,500 MW, - using the sub-technologies: metering the fuel, gasification reaction in a gasification reactor with a cooled reaction chamber contour, quench cooling, raw gas washing, partial condensation, - a fuel dust with a water content <10% and a grain size <200 µm is given to several synchronized metering systems that feed the fuel dust via conveyor pipes (1.4) to several gasification burners (2.1) arranged at the head of a reactor (2), which are arranged symmetrically and contain additional oxygen feeds, - the ignition increases rerer dust burner (2.1) with oxygen supply in the head of the gasification reactor (2) by means of pilot and pilot burner (2.2), - a quantitative recording of the fuel dust and oxygen supplied to the dust burners (2.1) takes place, the total of all the supplied amounts of fuel dust and oxygen is recorded and a control mechanism ensures that the oxygen ratio does not fall below or exceed the ratio of 0.35 to 0.65, regardless of the fuel dust and oxygen distribution to the burners (2.1), - the fuel dust in the gasification reactor (2) at temperatures between 1,200 and 1,900 ° C and at pressures between ambient pressure and 8 MPa is converted into a raw synthesis gas and a slag, - the 1,200 to 1,900 ° C hot raw gas and the slag together in a quench cooler (3) by injecting water to the dew point at temperatures between 180 ° C and 240 ° C are cooled and - the cooled raw gas further treatment stages such as water washing, part ondensation or catalytic processes. Procedure according to Claim 13 , characterized in that three metering systems (1) direct fluidized fuel dust flows via delivery pipes (1, 3) to three dust burners (2.1). Method according to one of the preceding Claims 13 to 14 , characterized in that the grain size of the fuel dust is <100 µm. Method according to one of the preceding Claims 13 to 15 , characterized in that the water content of the fuel dust is <2% by mass. Method according to one of the preceding Claims 13 to 16 , characterized in that the fuel dust is supplied as a fuel dust-water slurry, each burner (2.1) having its own feed system. Method according to one of the preceding Claims 13 to 17th , characterized in that the fuel dust is fed to the gasification reactor (2) as a fuel dust-oil slurry, the burner (2.1) having its own feed system. Method according to one of the preceding Claims 13 to 18th , characterized in that several types of fuel are gasified at the same time. Method according to one of the preceding Claims 13 to 19th , characterized in that a different fuel is gasified over each gasification burner (2.1). Method according to one of the preceding Claims 13 to 20 , characterized in that the gasification burners (2.1) are gasified pneumatically or as slurry fuel dusts.

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