DE102008012734A1 - Method for obtaining synthesis gas by gasification of liquid or finely comminuted solid fuels, involves producing synthesis gas in reaction chamber arranged over reactor, in which ingredients are supplied - Google Patents

Abstract

The method involves producing synthesis gas in reaction chamber (2) arranged over the reactor (3), in which ingredients are supplied in its upper area. Another area is bounded by a water film, which is produced by suitable devices. The generated and cooled synthesis gas is withdrawn from the pressure container (4). An independent claim is included for a gasification reactor for obtaining synthesis gas by the gasification of liquid or finely comminuted, solid fuels.

Description

The The invention relates to a method and a device for the gasification of both finely divided fuels, eg. B. dusty Fuels from coal, petroleum coke, biological waste fuels, as well as liquid fuels, such as oil, Tar, refinery residues and other liquid Residues that atomises in the carburetor can be used to generate synthesis gas.

Methods and devices of this type are known in large numbers. For example, designs with slag drain in the bottom and gas outlet at the top are known. The US 3,963,457 describes a Koppers Totzek gasifier with horizontal, opposed burners, bottom slag effluent, gas effluent and gas quench above, and a recooled, cooled gas process. The EP 0 400 740 B1 describes a shell gasifier with horizontal burner, bottom slag discharge, top gas outlet and gas quench upward, equipped with vertical mixing tube. The US 4,936,871 describes a Koppers carburettor with gas outlet at the top and upwards gas quench also equipped with a vertical mixing tube. The US 5,441,547 describes a PRENFLO carburetor with also a gas outlet top and upward gas quench, equipped also with vertical mixing tube, also a deflection and heat exchanger downwards. The US 4,950,308 describes a Krupp-Koppers gasifier with horizontal burner, slag outlet at the bottom, gas outlet at the top, furthermore equipped with radiant cooler and gas quench. Most Koppers-Totzek carburetors had a water quench which caused cooling to about 1000 ° C, which was far from the dew point of the gas produced, with nozzles producing a water spray.

adversely These technologies were the high design and the lack of Suitability for further cooling of the generated Synthesis gas. If you had a water quench with excess water want to use a cooling of the synthesis gas up to reach the dew point would have risked that water would be in the burner level below which is very risky in terms of safety would have been. Furthermore, there would have been thermodynamic disadvantages if quench water had entered the reaction zone of the carburettor.

Also known are designs with carburetor, in which the exit of the synthesis gas and the slag take place through a hole in the bottom and which are equipped with a water quench with dip tube. For example, this describes US 4,247,302 a Texaco carburetor with top burner and bottom joint gas and slag exit. Beneath the gasifier is a separation vessel from which slag falls down into slag bath while the synthesis gas flows sideways into a gas quench vessel. The disadvantage is that several containers are required and there is a tendency to block because hot, not yet solidified slag particles must be promoted, especially in the pipeline from the separation vessel to the quench container.

In the US 4,494,963 is a Texaco carburetor described above with burner arranged and common exit of gas and slag down. Below the carburetor is a liquid quench consisting essentially of a with coolant, z. As water, wetted and immersed in the bath tube. A similar procedure is also used in the EP 0 278 063 A2 described. In the EP 0 374 324 A1 describes how such a dip tube is additionally wetted with liquid inside. Further examples of similar embodiments are given in the documents US 4,992,081 and US 5,744,067 shown.

By the use of a wetted with a liquid film Immersion tube deposits are prevented. This liquid film adheres to the wall, moves vertically, cools and prevents Formation of deposits. A disadvantage of these concepts, however, that the quench outlet temperature of the size and the residence time of the gas bubbles in the water bath depends, which in turn are influenced by several factors, e.g. B. gas flow, pressure, Solids content in a water bath, causing fluctuations in the outlet temperature result in and achieve no efficient excretion of fly ash leaves. Further, the lower end of the submerged pipe alternating with very hot gas and with water in contact, resulting in faster material fatigue and formation of deposits leads.

Carburetor types are also known in which both the synthesis gas produced and the slag are conducted downwards and a spray quench is provided for cooling. For example, this describes DE 40 01 739 A1 such a carburetor. Under the carburetor, water is sprayed onto the hot gas at different levels in the form of spray cones. The cooled gas leaves the quench zone sideways and the slag falls into a water bath. A similar technology is also used in the WO 98/45388 A2 described.

The DE 10 2005 048 488 A1 describes a system with several symmetrically arranged burners at the reactor head; wherein generated synthesis gas and slag are treated together in a quench cooler by water injection to the dew point, which is between 180 ° C and 240 ° C, or by partial cooling with waste heat utilization. In the DE 10 2005 041 930 A1 describes how slag and raw gas are discharged together below, with one or more annular rows of nozzles injecting condensate water; the slag is discharged through a water bath. The dust is removed at the end of the quench chamber. In the DE 10 2005 041 931 A1 Furthermore, a Teilquenchen is described by arranged in the jacket nozzles with condensate water with cooling to about 700-1100 ° C; This is followed by a waste heat boiler.

The DE 197 51 889 C1 describes a gasification process in which the hot gases leaving the gasifier are cooled via a quench nozzle. Ash leaves the reactor via an intensively cooled slag exhaust and is cooled and washed in the quench. The quench nozzle has a drainage edge for slag; intensive mixing is achieved by a constriction in the quench nozzle. The slag is then discharged and cleaned of soot. In the EP 0 084 343 A1 is described a down acting against a water bath coal gasifier with two-stage quench, the first quench is located directly after the carburetor. The US 2007 006 2117 A1 describes a similar process.

adversely is in this process that of the downflow hot gas jet and the water droplets from nozzles create intense circulation in the quench room, causing water droplets distributed throughout the room. The drops of water in the area the slag hole cools the slag so hard, that their surface solidifies and stalactites are formed. The fine slag particles and water droplets form deposits on the walls, which are not wetted with a water film, So dry walls, ceiling, nozzles, in particular in places that are alternately moist and dry. Always when Water evaporates on the wall, becoming deposits of impurities educated. The stalactites and deposits result in the Consequence to considerable operational problems.

Gasification processes are also described in which the synthesis gas produced and the slag are fed separately downwards. For example, this describes DE 197 18 131 A1 How are separated gasification gas and melt, especially a molten salt as a special form of slag, separated. The synthesis gas is cooled in a discharge device by injecting water or saline solution via nozzles. The melt is led into a private bath and treated accordingly.

The The object of the invention is therefore a simple and economical Gasification process and a matching device for extraction of synthesis gas by gasification of liquid or fine divided, solid fuels under a pressure of 0.3 to 8 MPa at a temperature in the range of 1200 to 2000 ° C. with oxygen-containing gaseous gasification agents in a cooled reactor, on the walls of which liquid Slag is separated and which is located in a pressure vessel, to provide, which no longer the disadvantages described having.

• • das erzeugte Synthesegas in einem ersten, oben im Reaktor angeordneten Reaktionsraum erzeugt wird,
• • in dessen oberen Bereich die Einsatzstoffe zugeführt werden,
• • an dessen Seitenwänden flüssige Schlacke niedergeschlagen wird, die frei ablaufen kann, ohne dass die Oberfläche dieser Schlacke dabei erstarrt,
• • und an dessen Unterseite sich eine Öffnung mit einer Abtropfkante befindet, aus der sowohl das gewonnene Synthesegas nach unten abgezogen wird als auch die flüssig herablaufende Schlacke abtropfen kann,
• • sich unten an die Öffnung ein zweiter Raum anschließt, in dem das Synthesegas trocken gehalten und abgekühlt wird, und
• • der zweite Raum durch einen Wasserfilm begrenzt wird, der durch geeignete Vorrichtungen erzeugt ist und frei fällt,
• • sich unten an den zweiten Raum ein dritter Raum anschließt, in dem durch Zufuhr von Wasser in das Synthesegas eine Abkühlung vorgenommen wird,
• • sich unten an den dritten Raum ein Wasserbad anschließt, in welches die abgetropften und bereits erstarrten oder noch flüssigen Schlacketeilchen hineinfallen,
• • und unten oder seitlich des dritten Raums, jedoch oberhalb des Wasserbades das erzeugte und abgekühlte Synthesegas aus dem Druckbehälter abgezogen wird.

The invention solves the problem by

• The generated synthesis gas is generated in a first reaction space arranged at the top of the reactor,
• • in the upper area of which feedstocks are supplied,
• • on whose side walls liquid slag is deposited, which can run freely without the surface of this slag solidifies,
• • and on the underside of which there is an opening with a drip edge, from which both the recovered synthesis gas can be drawn down and the liquid draining slag can drip off,
• • At the bottom of the opening, there is a second space, in which the syngas is kept dry and cooled, and
• The second space is bounded by a film of water generated by suitable devices and falling freely,
• • a third room adjoins the second room at the bottom, in which a cooling is carried out by supplying water into the synthesis gas,
• • at the bottom of the third room there is a water bath into which the dewatered and already solidified or still liquid slag particles fall,
• • and below or laterally of the third space, but above the water bath, the generated and cooled synthesis gas is withdrawn from the pressure vessel.

The gasification is preferably carried out in suspension at a low particle loading of less than 50 kg / m ³ - not in a fluidized bed - with oxygen-containing gasification agents and under elevated pressure at temperatures above the slag melting point, wherein the generated gas and deposited on walls slag the carburetor leave through an opening in the floor. Below the gasifier bottom, the gasification products pass through a hot, dry zone which is separated from the quench zone by means of a free-flowing water film to prevent circulation of the droplet-containing cold gas from the quench zone to the vicinity of the slag drainage edge.

In embodiments of the invention, coal, petroleum coke, biological waste, biological fuels or plastics in comminuted form are used as solid fuels. The solid fuel diameter should not exceed 0.5 mm. First, solids are pressurized in one or more parallel sluices by means of a non-condensable gas such as N ₂ or CO ₂ , which is 2 to 10 bar above the gasifier pressure. Then the solids are pneumatically conveyed from one or more feed containers in the carburetor, preferably as dense phase conveying. As liquid fuels, oil, tar, refinery residues or aqueous suspensions can be used. Most liquid fuels can be pumped into the carburettor, only with abrasive fluids is smuggling and pressure increase with a compressed gas preferable. A mixture of solid and liquid fuels is also possible. Flammable or pollutant gases can also be fed into the carburettor. At the high gasification temperatures, pollutants are thermally decomposed, with the solid reaction products being embedded in the glassy slag and the gaseous products leaving the gasifier as simple molecules such as H ₂ , CO, N ₂ , HCl or H ₂ S.

In Further embodiments of the invention, it is provided that the Gasification reaction carried out in a cloud of dust or drops becomes. Feeding of fuel and gasifying agents in the carburettor can by at least two on the side wall of the first reaction space with separate attachments mounted burners, alternatively or additionally, the supply of the fuel and the Gasification agent in the carburetor by at least one the ceiling of the gasification reactor burners take place. The gasification agent can before entering the reactor by Baffles or a special design of the burner with a Be provided swirl.

In Further embodiments of the invention, it is provided that the second space down through a funnel-shaped water film is limited, which falls freely and only by the downward Beam of the recovered synthesis gas is torn. Preferably The water film separating the second space from the third space is used accelerates a conically executed water ramp. For this should be provided that the water ramp by means of a shield protected against heat and dust. This shield may be a refrigerated device that separates the second room from an outdoor room and from this Outside space through a gaseous cooling medium or is acted upon by a water wetting.

Out a closed film does not escape any drops of water and the Surface of the water film is several orders of magnitude smaller than that of a nozzle-generated drop spectrum, thereby the predominantly caused by evaporation cooling effect is weak. The environment of the slag drip edge remains with it Water-drop-free and hot, allowing solidification of the slag can be excluded directly on the drip edge, which is an advantage of the invention. Because the gas atmosphere in the second room remains dry in this way, there are no deposits formed by evaporation of water on the wall.

In Further embodiments of the invention, it is provided that the third room is provided with a vertical partition and the first obtained synthesis gas in the formed by the partition wall inner region flows downward, then deflected is and in the outer wall formed by the partition Area upstream flows before it the pressure vessel leaves. The partition should be inside and outside be wetted with water.

In Further embodiments of the invention is provided that below arranged water bath generates a circulation flow becomes. Preferably, all the water used should be acidified become. Furthermore, it can be provided that the water from the Water bath with suitable pumping medium in the third room returned and used for the formation of the water film.

• • einen ersten, oben im Reaktor angeordneten Reaktionsraum,
• • in dessen oberen Bereich eine Zuführvorrichtung für Einsatzstoffe angeordnet ist,
• • dessen Seitenwände mit Rohren mit Innenkühlung als Membranwand oder Rohrschlangen ausgestattet sind, an denen flüssige Schlacke frei ablaufen kann, ohne dass die Oberfläche dieser Schlacke dabei erstarrt,
• • und an dessen Unterseite eine Öffnung mit einer Abtropfkante vorgesehen wird,
• • sich unten an die Öffnung ein zweiter Raum anschließt, in dem das Synthesegas trocken gehalten und durch Strahlungskühlung abgekühlt wird, und
• • eine Vorrichtung zur Erzeugung eines Wasserfilms vorgesehen wird,
• • sich unten an den zweiten Raum ein dritter Raum anschließt, in dem Zuführeinrichtungen für Wasser vorgesehen sind,
• • sich unten an den dritten Raum eine Aufnahmeeinrichtung für ein Wasserbad anschließt, welches auch eine Abzugsvorrichtung für eine Wasser-Schlacke-Gemisch aufweist,
• • und unten oder seitlich des dritten Raums eine Abzugsvorrichtung für Synthesegas aus dem Reaktor vorgesehen ist.

The invention also relates to the gasification reactor for carrying out the described method, comprising

• A first reaction space arranged at the top of the reactor,
• A feed device for feedstocks is arranged in the upper region thereof,
• • whose side walls are equipped with tubes with internal cooling as diaphragm wall or pipe coils, where liquid slag can drain freely, without the surface of this slag solidifies,
• • and on the underside of which an opening with a drip edge is provided,
• • a second space adjoins the opening at the bottom, in which the synthesis gas is kept dry and cooled by radiation cooling, and
• A device for producing a water film is provided,
• • a third room adjoins the second room at the bottom, in which water supply devices are provided,
• • Connected to the bottom of the third room a receiving device for a water bath, which is also a trigger for a What Ser-slag mixture,
• • And below or laterally of the third space, a discharge device for syngas from the reactor is provided.

In Further embodiments of the invention is provided that at least two burners on the side wall of the first reaction chamber with separate Attachments are attached. The burners are preferably in the space sekantial with a horizontal angle to 20 ° and aligned at a vertical angle to 45 °. Furthermore, can be provided that at least one burner on the ceiling of the Gasification reactor is attached.

In Further embodiments of the invention is a conically executed Water ramp provided between the second and third room, with between the second reaction space and the water ramp, a device for Shield is attached.

In A further embodiment of the invention provides that in the third room a vertical partition is attached.

In A further embodiment of the invention provides that the receiving device for the water bath a central Slag storage tank and an annulus for having fine dust laden water.

The Invention will be described in more detail below with reference to 2 examples explained.

1 shows a gasification reactor according to the invention schematically in longitudinal section

2 shows an alternative design of the lower part of the gasification reactor according to the invention

The However, the invention is not limited to these two embodiments limited.

The gasification of the fuel takes place with an oxygen-containing gasification agent in the reaction space 2 under pressure (0.3-8 MPa) and above the ash melting point at temperatures of 1200-2500 ° C. The cooled reaction vessel 3 protects the pressure vessel 4 before high temperatures. In the annulus 32 In continuous operation, a small stream of cold gas, eg. As nitrogen, fed. The room is in front of the hot gas through a water lock 30 protected. With rapid pressure increase in the reaction space 2 However, the hot gas can also enter the annulus 32 penetration. To the pressure vessel 4 To protect against warming during a temporary or accidental inflow of hot gas, its inner wall is thermally insulated. Fuel, reactants, and optional wastes to be disposed of are provided via at least two laterally located burners 5 fed.

Liquid, on the walls of the reaction vessel 3 separated slag flows along the wall to the exit opening 6 , separates from the drip edge 7 and falls as a drop or jet in the water bath 21 , The generated, dust-containing gas also flows out of the reaction space through the opening 6 first through a hot and dry room 8th in the wet Quenchraum 15 , To a back flow of the cold, drop-containing gas from the quench 15 in the hot room 8th to avoid being a water film 12 with the water distributor 28 and the conical ramp 11 generated, which flows concentrically into the gas space. This movie will only be released through the opening 6 torn downwards flowing hot gas or slag jet.

With the internally cooled with a cooling medium or externally by an adherent film of water and optionally cleaned with beaters shield 9 becomes the ramp 11 and the space above 10 protected from high thermal load and from dust, whereby the formation of deposits in this room is largely avoided. The water film, which is a few millimeters thick, breaks down into drops that evaporate or evaporate, intensively cooling the hot gas. The inflow of water, which forms the water film, is always greater than the amount of water consumed by evaporation or evaporation. The excess water helps the partition 14 of the quenching room 15 to moisten and wash out solid particles from the gas.

The vertical walls in this area can be additionally water by the water supply 27 over an overflow as well as with the nozzles 16 be wetted. With nozzles that produce a fine droplet spectrum, the cooling of the gas and the washing out of the fly ash can also be intensified. No support surface for deposits in the quenching chamber 15 with high dust loading, there will be nozzles 16 in the wall 14 integrated. Through the gap 19 the cooled gas gets into the annulus 17 directed. The gas deflection by 180 ° and low upward speed in the annulus favor the separation of coarse ash particles and water droplets. Also in this room is water spray by means of the nozzles 18 injected, mainly to wash out the dust.

Due to the gas outlet 13 or the nozzle, the gas flow in the quench and annulus is asymmetrical, which locally increased velocities in the annulus and increased discharge of Fluga caused. With uniform injection of the water spray into the annulus, the floating drops of water cause approximately the same pressure loss in the entire ring cross-section, which contributes to the homogenization of the gas flow in the annulus.

Below the flow deflection through the gap 19 is in a water bath 21 a slag storage tank 23 Installed. This is with concentrically arranged nozzles 26 equipped, so that coarser slag particles can be additionally intensively cooled. These nozzles are via a ring manifold 25 supplied with water, which is arranged outside of the slag collecting container and into the water bath 21 with the help of other nozzles 24 induced a flow, so that deposits are avoided.

About the slag discharge 22 The slag is transferred via a slag crusher into a slag sluice, in which it is cooled by means of process water to about 60 ° C and then discharged via a slag extractor from the process.

In a typical operation case, 50 kg / s of dried and ground lignite are gasified at 40 bar and 1500 ° C, which corresponds to a chemical conversion of 1 GW. Here, 85 kg / s of synthesis gas are recovered, with 1 kg / s fly ash and 3 kg / s liquid slag incurred. For quenching 70 kg / s of water are evaporated, in the water film 140 kg / s of water are fed, the non-evaporated water runs together with the water for wetting the wettable surfaces in the water and over the nozzles of the water drain 20 withdrawn and by means of a circulation pump to the various feed points 16 . 18 . 25 . 27 . 28 is returned in the quench area. For the separation of fly ash in the annulus 17 a total of 24 full cone nozzles 18 built in two levels with a total water throughput of 160 kg / s. The water also runs into the water bath.

2 shows an alternative design of the second and third room. This is a particularly steep acceleration ramp 11 intended. A shield of the acceleration ramp can therefore be omitted as well as the partition in the third room. The freely falling water film separates the hot and drip-free central space 8th from the cold, damp room 15 whereby a circulation of the drop-containing synthesis gas in the vicinity of the slag drainage edge and thus too intensive cooling of the slag hanging on the slag drainage edge is avoided. The oval, dashed lines in 2 show the separate circulations in the hot and in the damp room. The falling water film has only a negligible radial velocity component, hence the hot, dry space 8th only by spreading the out of the outlet 6 closed gas jet, whereby this space is longer than radially fed water film. Optionally, water can be sprayed through nozzles mounted between the falling surface of the water film and the pressure vessel. Intensive radial injection of the quench water should only below the line of intersection of the falling surface of the water film with the lateral surface of the propagating out of the outlet opening 6 outflowing gas jet done.

1

manhole

2

reaction chamber of the carburetor

3

reactor vessel

4

pressure vessel

5

burner

6

outlet opening for gasification products

7

Schlackeabtropfkante

8th

room with hot dry gas

9

shielding

10

room with cold gas

11

conical Acceleration ramp for water film

12

water film in free fall

13

gas outlet

14

With Water wetted partition

15

quench

16

jet integrated in the partition

17

annulus (below)

18

jet

19

gap

20

water drainage

21

water bath

22

slag discharge

23

slag collection container

24

initiator circulation flow

25

ring distributor

26

Concentric arranged nozzles

27

water supply for wall film

28

water supply for water film

29

water supply for moated castle

30

water Castle

31

Divider

32

annulus (above)

QUOTES INCLUDE IN THE DESCRIPTION

This list The documents listed by the applicant have been automated generated and is solely for better information recorded by the reader. The list is not part of the German Patent or utility model application. The DPMA takes over no liability for any errors or omissions.

Cited patent literature

• US 3963457 [0002]
• - EP 0400740 B1 [0002]
• US 4936871 [0002]
• US 5441547 [0002]
• US 4950308 [0002]
• - US 4247302 [0004]
• US 4494963 [0005]
• EP 0278063 A2 [0005]
• EP 0374324 A1 [0005]
• - US 4992081 [0005]
• US 5744067 [0005]
• - DE 4001739 A1 [0007]
• WO 98/45388 A2 [0007]
• - DE 102005048488 A1 [0008]
• DE 102005041930 A1 [0008]
• DE 102005041931 A1 [0008]
• - DE 19751889 C1 [0009]
• EP 0084343 A1 [0009]
• US 20070062117 A1 [0009]
• DE 19718131 A1 [0011]

Claims (25)

A process for the production of synthesis gas by gasification of liquid or finely divided solid fuels under a pressure of 0.3 to 8 MPa at a temperature in the range of 1200 to 2000 ° C with oxygenated gaseous gasification agents in a cooled reactor, on the walls of which liquid Slag is deposited and which is located in a pressure vessel, characterized in that • the generated synthesis gas is generated in a first, arranged in the top of the reactor reaction space, • in the upper region of the feedstock are fed, • on the side walls of liquid slag is deposited, which can run freely without the surface of this slag solidifies, • and on the underside of which there is an opening with a drip edge, from which both the recovered synthesis gas is withdrawn down and the liquid running down slag can drain, • down to the opening a second room ansc in which the synthesis gas is kept dry and cooled, and • the second space is bounded by a water film, which is generated by suitable devices and falls freely, • connects to the second space at the bottom of a third space, in which by feeding Water in the synthesis gas is cooled down, • connects down to the third room a water bath, in which the drained and already solidified or still liquid slag particles fall into it, • and bottom or side of the third room, but above the water bath, the generated and cooled Synthesis gas is withdrawn from the pressure vessel. Method according to claim 1, characterized in that that as solid fuels coal, petcoke, biological waste, Biological fuels or plastics are used in crushed form. Method according to claim 1, characterized in that that the diameters of the solid fuels do not exceed 0.5 mm. Method according to claim 1, characterized in that that as liquid fuels oil, tar, refinery residues or aqueous suspensions are used. Method according to one of claims 1 to 4, characterized in that the gasification reaction in a Dust or drop cloud is performed. Method according to one of claims 1 to 5, characterized in that the supply of the fuel and the Gasification agent in the carburetor by at least two on the sidewall the first reaction chamber attached with separate fasteners Burners take place, with the burners in one or more levels to be ordered Method according to one of claims 1 to 5, characterized in that the supply of the fuel and the Gasification agent in the carburetor through at least one on the ceiling the burner located in the gasification reactor takes place. Method according to one of claims 1 to 7, characterized in that the gasification means before entry into the reactor through baffles or a special design of the Brenners be provided with a twist. Method according to one of claims 1 to 8, characterized in that the second space down through limited to a funnel-shaped or cylindrical water film becomes, which falls freely and only by the downward Beam of the recovered synthesis gas is torn Method according to one of claims 1 to 9, characterized in that the water film, the second Room separates from the third room, by means of a conical running Water ramp is accelerated. Method according to claim 10, characterized in that that the water ramp is shielded from heat and dust pollution is protected. Method according to claim 11, characterized in that that the shield is a cooled device that separates the second room from an outside room and from this one Outside space through a gaseous cooling medium or is acted upon by a water wetting. Method according to one of claims 1 to 12, characterized in that the third space with a vertical Partition is provided and the recovered synthesis gas first flows downwards in the inner area formed by the partition wall, is then deflected and formed in the outer wall formed by the partition Area upstream flows before it the pressure vessel leaves. Method according to claim 13, characterized in that that the partition wall wets with water from inside and outside becomes. A method according to claim 1, characterized in that in the below arranged water bath a circulation flow is generated. Method according to one of claims 1 to 15, characterized in that the water from the water bath with suitable Pumping means returned to the third room and is used for the formation of the water film Method according to claim 1, characterized in that that the used water is acidified. Gasification reactor for carrying out the method according to claims 1 to 17, characterized by • one first, arranged at the top of the reactor reaction space, • in whose upper part is a feed device for feedstocks is arranged • its side walls with Tubes with internal cooling as a membrane wall or pipe coils are equipped, run on which liquid slag freely can, without the surface of this slag solidifies, • and on the underside of an opening with a drip edge is provided • down to the opening a second room adjoins, in which the syngas dry kept and cooled by radiation cooling will, and • Provided a device for producing a water film becomes, • at the bottom of the second room a third Room adjoins, in the feeder facilities for Water are provided, • down to the third Room connects a receiving device for a water bath, which also has a trigger for a water-slag mixture having, • and below or to the side of the third room provided a discharge device for synthesis gas from the reactor is. Device according to claim 18, characterized in that that at least two burners on the side wall of the first reaction space are attached with separate fasteners. Device according to claim 19, characterized in that that the burners are aligned in the space sekantial with a horizontal angle up to 20 ° and a vertical angle up to 45 ° Device according to claim 18, characterized in that that at least one burner on the ceiling of the gasification reactor is appropriate. Device according to one of claims 18 to 21, characterized in that a conically executed Water ramp between the second and third space is provided. Device according to claim 22, characterized in that that between the second reaction space and the water ramp one Shielding device is attached. Device according to one of claims 18 to 23, characterized in that in the third space a vertical Partition is attached. Device according to one of claims 18 to 24, characterized in that the receiving device for the water bath has a central slag storage tank and has an annular space for fine dust laden water.