DE102007006984B4 - Process and apparatus for the conversion of raw gases in the flow stream gasification - Google Patents

Abstract

Process for the conversion of raw gases of the entrained flow gasification of carbonaceous feedstocks under pressure, wherein the withdrawn from a Flugstromvergaser hot raw gases are injected in a downward flow in a Quenchraum whose upper part is formed as a gas space and the lower part of a water bath, the lower limit of Gas space is formed by the water surface of the water bath, wherein quench water is injected and the raw gases are cooled and the raw gases are withdrawn above the water bath from the gas space, characterized
- That water is only injected into the gas space, which surrounds the downward flow of the withdrawn from the entrained flow gasifier hot raw gases, so that the above the water surface upwardly deflected raw gases are humidified and cooled before they interfere in the downward flow .
- That the entrained with the raw gases minor components by means of these raw gases during cooling in the central zone of the downward flow and during the ...

Description

The The invention relates to a method and a device for conversion of raw gases at the entrainment gasification.

The hot raw gases produced in the stream gasification must be cooled before their further use. In the case of the gasification of ash-containing fuels, the secondary components entrained with the raw gases containing about 1400 to 1600 ° C. make the cooling process more difficult. As minor constituents, the molten and condensable constituents and optionally unreacted residual carbon are understood. The secondary components in the indirect cooling lead to the laying of heat exchangers and to corrosion. The cooling is therefore carried out in the simplest case by direct quenching of the hot raw gases with water. For entrained flow gasifiers according to the GSP method (Higman, Chris; Gasification, Elsevier Science, 2003), the quench space is arranged directly below the gasifier, in which water is injected into the hot raw gases and cooled abruptly to the steam dew point. The quench cooling has the disadvantage that no medium or high pressure steam is generated, which can be energetically used in the steam turbine. However, it is much cheaper and störungsunanfälliger in operation. Benefits arise when the further use of the raw gas requires an increase in the water vapor content in the gas, such. B. for the conversion of carbon monoxide CO with water vapor H ₂ O to carbon dioxide CO ₂ and hydrogen H ₂ according to the equation CO + H ₂ O = CO ₂ + H ₂ . The quench cooling to Wasserdampftaupunkt then provides for the provision of the water vapor required for the conversion reaction. The disadvantage here is that the quenched raw gases must be reheated.

For the flow stream gasification after the GSP procedure is about it addition, a proposal for a so-called partial quench known. In the entering into the Quenchraum about 1400 ° C hot raw gases should only injected as much water be that the quenched raw gases with a gas outlet temperature from about 800 ° C leave the quench room. This is a partial chemical reaction of CO with water vapor after the above-described conversion reaction respectively. Since the direct quenching of the hot raw gases predominantly take place in the core stream with abrupt temperature reduction should, the chemical conversion within the shortest possible time Time to come to a halt, so that the chemical turnover remain low becomes. This solution proposal is also very disadvantageous, since circulation flows of high temperatures> 800 ° C occur in the quenching chamber, the to an undesirable occupancy the walls that surround the quench room with condensing constituents and solidifying slag droplets. The Occupations can into the downstream facilities for raw gas cooling and continue treatment and lead to severe malfunctions.

US 2,961,310 A discloses a method and apparatus for producing synthesis gas in which the raw gas is to be quenched by venting a fuel-water slurry to temperatures of about 500 ° F (260 ° C) prior to exiting the gasifier. The subsequent further cooling to the water vapor saturation temperature, combined with water scrubbing, takes place in a scrubber. The expert is unequivocally clear that at these low temperatures, the conversion reaction does not take place in principle, regardless of what type and gradation of the water supply is selected.

DE 41 09 231 C2 relates to a process for the utilization of halogenated carbonaceous wastes. Crude gases are transferred to a conversion reactor, wherein in the inflowing raw gas is injected via a nozzle cross water vapor and NaOH. It is therefore a classic Quenchung with sudden cooling of the raw gas to the Wasserdampftaupunkt, ie to a Vollquench, wherein only a portion of the water is evaporated, ie, water is added significantly in excess. The conversion reaction is practically excluded under these conditions.

US 4,479,809 A describes a high-pressure coal gasifier with Schlackeabscheideraum to which a slag droplets loaded raw gas is supplied via an inlet pipe. In order to cool the crude gas and deposit the slag in a water bath, cold raw gas is introduced into the gas stream. By introducing this gas having a water vapor content which is less than or at most equal to that of the hot raw gas, the conversion reaction is suppressed due to deficiency of water vapor. In the subsequent flow diversion over the water bath, which is accompanied by a humidification, but the temperature is already too low, that the conversion reaction could take place to any significant extent.

DE 10 2006 031816 A1 discloses a method and apparatus for cooling hot gases and liquefied slag in runoff gasification. In this case, the cooling water introduced for cooling is divided, wherein a part injected into the raw gas inlet and another part is used to cool the container wall. Here, again, a modification of the classical variant of Vollquenches for the GSP entrained flow gasification process is described, in which the gasification gas immediately is cooled after exiting the reactor 2 to the water vapor saturation temperature of 180 to 240 ° C. By thus intended and achieved rapid cooling, the conversion reaction is effectively suppressed.

There are further proposed solutions for connecting the process steps of the quenching and the conversion to the so-called quench conversion, in which the conversion reaction is carried out non-catalytically during the cooling of the raw gases in one step. Ullmann's Encyclopedia of Industrial Chemistry (2003), Vol.15, p.387 describes an example of the cooling of a raw gas of the asphalt gasification of 1570 ° C with the supply of water, in which the conversion equilibrium at 1250 ° C is established. According to patent DE 43 18 444 C2 The conversion in the temperature range 700 to 900 ° C should take place by using quench water. Provided are still indirect heat exchangers. The high expenditure on equipment and the thereby achievable relatively low conversion conversions have meant that the technical application of the method in the entrained flow gasification of ash-containing fuels has not been achieved so far.

task The invention is the quench conversion process for entrainment gasification to improve so that in the downstream of the air flow gasifier Quenchraum the conversion with the least amount of equipment can be achieved.

• – dass Wasser nur in den Gasraum eingedüst wird, der die nach unten gerichtete Strömung der aus dem Flugstromvergaser abgezogenen heißen Rohgase umschließt, so dass die oberhalb der Wasseroberfläche nach oben umgelenkten Rohgase befeuchtet und gekühlt werden, bevor sie sich in die nach unten gerichtete Strömung einmischen,
• – dass die mit den Rohgasen mitgeführten Nebenbestandteile mittels dieser Rohgase während der Abkühlung in der zentralen Zone der Abwärtsströmung und während der Befeuchtung und Kühlung in der ringförmigen Zone der Aufwärtsströmung bei gleichzeitiger Anreicherung der im Gasraum in der Schwebe gehaltenen festen und kondensierbaren Nebenbestandteile mit den Rohgasen katalytisch aktiviert werden,
• – und dass die Umfassungswände des Quenchraumes, mindestens jedoch die Umfassungswände des Gasraumes so gekühlt werden, dass die Temperatur an der inneren Oberfläche 1 bis 50 K unterhalb der Taupunkttemperatur des Gasraumes liegt.

The object of the invention is for entrained flow gasifier, the raw gases are introduced in a downward flow in a quench, the upper part is formed as a gas space and the lower part of a water bath, wherein the lower boundary of the gas space is formed by the water surface of the water bath, wherein quench water is injected into the downward flow and the raw gases are cooled and the raw gases are withdrawn above the water bath from the gas space, thereby solved

• - That water is only injected into the gas space, which surrounds the downward flow of the withdrawn from the entrained flow gasifier hot raw gases, so that the above the water surface upwardly deflected raw gases are humidified and cooled before they interfere in the downward flow .
• - That the entrained with the raw gases minor components by means of these raw gases during cooling in the central zone of the downward flow and during humidification and cooling in the annular zone of the upward flow with simultaneous enrichment of the gas space suspended in the supernatant solid and condensable minor components with the raw gases to be activated,
• - And that the enclosure walls of the quench, but at least the surrounding walls of the gas space are cooled so that the temperature at the inner surface is 1 to 50 K below the dew point temperature of the gas space.

According to the invention in the gas space two flow zones aerodynamically designed, a central zone of the downward flow of the raw gases and an annular zone the upward flow of the converted Raw gases surrounding the central zone and reaching to the surrounding walls and into which the water was injected with which the upward flowing gases chilled and moistened. In the central zone of the downward flow will be the raw gases rectified to the cooling-related density gradient and in the zone of upward flow the cooling-related Density gradients led. This leads to a stabilization of the downward flow with interference of the moistened and cooled Gases from the upward flow. The Downstream is according to the invention in comparison to the previously in the full and partial quenching subsequent shock-like cooling by water injection in the hot Crude gases cooled with a significantly lower temperature gradient (delayed cooling).

The Speed of the conversion reaction is under these conditions in the central zone of the downward flow over their total vertical extent very high, as high and in the flow direction steadily decreasing temperatures with water vapor levels increasing in the direction of flow be combined. The in the flow direction increasing water vapor levels in the downflow are adjusted thereby that the cooled and humidified gases of upflow in mixed in the downflow become. Thus, the conversion reaction becomes in the central zone the downward flow up for deflection at the surface the water bath largely completed. The converted raw gases are while the deflection and then in the annular zone of the upward flow with simultaneous strong cooling loaded with water vapor. The increase the water vapor concentration is effected by evaporation of water the water surface of the water bath and by injection from water to the upward flow.

Another central part of the invention is the catalytic activation of the associated with the raw gases minor components by means of these raw gases during cooling in the central zone of the downward flow and during humidification in the annular zone of upward flow with simultaneous enrichment held in the gas space in suspension, activated minor components. The catalytic activation of these secondary constituents is a complex process, which consists of various individual processes that complement each other, such as the surface enlargement of the catalytically active slag constituents, the reduction of metal oxides, the formation of porous condensation particles, the preservation of finest particles of unreacted residual carbon and the creation of high concentrations of volatile salts in the gas phase. In the following, these individual processes can only be hinted at.

In the central zone of the downward flow, the catalytic activation takes place by the more or less continuous cooling in a strictly reducing gas atmosphere without appreciable contact with water. Unlike wet cooling with quench water, the molten slag is more strongly atomized before it solidifies, creating a larger outer surface. The slag surface is also greatly reduced by carbon monoxide CO and hydrogen H _{2 of} the raw gases. It has a low degree of oxidation, ie it contains in comparison to wet-quenched particles whose surface is oxidized by condensate water (oxide skin), significantly more catalytically active metallic, oxidic and sulfidic compounds such. As iron / iron oxide (Wustit) / iron sulfide or heavy metals / heavy metal sulfides. The slag particles cool more slowly than the surrounding raw gases. This additionally increases the reaction rate of the conversion reaction catalyzed on the particle surface.

In the annular Zone of upward flow takes place the catalytic activation by condensation of alkali and Alkaline earth salts with the formation of very fine condensation nuclei and porous Condensation particle. These catalytically effective condensation particles are mixed into the downflow and especially effective there. Finest particles from unreacted Residual carbon, which circulate between the two flow zones catalyze the conversion reaction in the entire gas space. This is true in something modified way also for the gaseous Alkaline compounds due to the high temperatures in the zone the downward flow as far as possible are fleeting and catalyze the conversion reaction homogeneously.

To an advantageous embodiment of the method according to the invention is injected with so much water, that the raw gas leaving the gas space temperatures of 300 to 600 ° C or from 600 to 900 ° C exhibit.

It Two different temperature ranges are to be distinguished in which the procedure preferably performed becomes. In the lower temperature range 300-600 ° C maximum conversion levels the conversion reaction (about 30%) independently of the injected Water volume realized. With the amount of injected water is alone the desired gas outlet temperature regulated. In the upper temperature range 600-900 ° C submaximal, but variable Conversion rates of the conversion reaction (10-30% and above) are set. The amount of the injected Water is chosen according to the desired degree of conversion. When Measure of the degree of sales usually serves the gas composition measured online, leaving the gas space converted raw gases or from the material and energy balance indirectly determined value for the Degree of conversion. This is in the simplest case from the measured reactant streams and the gas outlet temperature calculated. By increased supply of water, the Gas outlet temperature lowered and the degree of conversion increased and vice versa. The execution of the process in the upper temperature range proves to be particularly advantageous. The high temperature exit converted raw gases can be fed to a waste heat boiler for steam generation. Besides that is it is possible with the help of the injected Amount of water to adjust the degree of conversion so that a desired Total conversion conversion in the conversion reactor after water washing, without that bypass the conversion reactor with a gas bypass or additional Water vapor available must be made.

The Limitation of the two temperature ranges results on the one hand the catalytic effect of activated minor components (lower Temperature limit) and on the other hand from the tendency to fouling minor components (upper temperature limit).

In the upper temperature range, the catalytic approximation of the gas composition to the thermodynamic equilibrium takes place. Depending on the physical and operational parameters and spatial arrangements present in the individual case, different approaches to the equilibrium composition can be achieved. The approximation is usually quantified in the form of the temperature approximation ΔT _K in Kelvin according to the equation ΔT _K = T _{G1, from} - T _out . T _{G1, from} the thermodynamic equilibrium temperature of the conversion reaction for the gas composition which sets at the gas outlet, and T _from the actual outlet temperature. Essential to the invention is that in the temperature range 1400 ° C to about 900 ° C, the temperature approximate ΔT _K not significantly differ from 0 K (about 0 to + 50 K) and further cooling to 600 ° C then to +100 to +250 K increase. At gas outlet temperatures below 900 ° C., the so-called kinetic reaction end temperature (700-850 ° C.) is reached, ie the conversion reaction "freezes." The further lowering of the gas outlet temperatures below the final kinetic reaction temperature by injection of water does not lead to any further change in the gas composition The lower limit of the cooling of the raw gases is about 300 ° C. At this lower temperature limit, the catalytic activation of the minor constituents is just ensured.The upper limit for the cooling of the raw gases is given by the critical temperature of the fouling tendency of the converted raw gases. The raw gases must be cooled down at least to the extent that deposits and contamination do not occur in the downstream plant components In difficult cases to at least 600 ° C, raw gas from the gasification of low-alkali and high-clay coal can be cooled to temperatures of at least 900 ° C.

The to increase the water vapor concentration and water needed for cooling is in a or more nozzle planes in the upward flow in nearby the surrounding walls of the gas space and as possible evenly distributed over the Injected circumference. The injection Preferably, by means of a nozzle plane above the water surface of the Water bath in the middle of the gas space or directed upwards. At carburetors big Performance will be more nozzle levels over the Height of Gas space distributed. For further top nozzle levels is the direction of the water atomization freely selectable, however, the injection is preferred upwards, which supports the upward gas flow. By the nozzle plane provided at the upper end of the gas space is preferably after the water sprayed down.

at low conversion conversion is the mean residence time the raw gases in the quenching room about 2 s and at high conversion conversion about 10 s.

Essential for the Invention is finally that the surrounding walls of the quench space, but at least the perimeter walls of the Gas room, cooled become. The cooling takes place such that the temperatures on the inner surface of the containment preferably set to values that are 1 to 50 K below the dew point temperature are in the gas space, making the walls permanent kept moist and permanent deposits of minor components be avoided. For energetic reasons, it makes sense behind the enclosure walls To produce saturated steam at a pressure of 5 to 10 bar (abs.). The efficiency the procedure will also increased if hot water injected , its temperature in the range of ± 50 K around the boiling point at Gasification pressure is. By injection of such preheated water local hypothermia is avoided to reduce the reaction rate of the conversion reaction would lead. It is also conceivable water that over the boiling temperature was heated, einzudösen. Overheated water mixed at the pressure atomization by spontaneous evaporation even faster with the raw gases in the gas space, whereby the reaction conversion increases further.

A special embodiment of the method relates to the reduction the distance between the surface of the water bath and the inlet opening the raw gases in the gas space to such a value that it is for spontaneous evaporation on the surface the water bath comes and the water injection for aftercooling completely omitted can be. The Rohgasaustrittstemperatur can then by means of ride height the water bath are regulated.

The converted raw gases are preferably at the lower end of the gas space deducted. They will be advantageous to an indirect heat exchanger supplied is generated in the medium pressure steam. Alternatively, the subsequent quenching with water until dew point possible.

According to the invention is it possible for the first time the desired conversion revenue with the least amount of equipment in the quench room of entrainment gasifiers to reach. Particularly noteworthy is the increase in the Cold gas efficiency. The efficiency of the gasification process and of the entire plant network of synthesis gas or power plants will be raised.

• – dass Quenchwasser nur in den Gasraum eingedüst wird, der die nach unten gerichtete Strömung der aus dem Flugstromvergaser abgezogenen heißen Rohgase umschließt, so dass die oberhalb der Wasseroberfläche nach oben umgelenkten Rohgase befeuchtet und gekühlt werden, bevor sie sich in die nach unten gerichtete Strömung einmischen,
• – dass die Umfassungswände des Quenchraumes, mindestens jedoch die Umfassungswände des Gasraumes so gekühlt werden, dass die Temperatur an der inneren Oberfläche 1 bis 50 K unterhalb der Taupunkttemperatur des Gasraumes liegt,
• – und dass der Quenchraum so bemessen ist, dass die mittlere Verweilzeit des Rohgases im Quenchraum 2 bis 10 s beträgt.

According to the invention the object is achieved by a device for the conversion of raw gases in the entrained flow gasification, which comprises an entrained Guage Quencheinrichtung with a Rohgaseintritt for downward flow of hot raw gases of the entrained flow gasifier and a gas outlet for converted raw gases, wherein surrounding walls surround a quench, consisting of a the downwardly directed inflow of the hot raw gas enclosing the gas space and a water bath, at least in one plane of the gas space extending nozzles for introducing quench water into the gas space and the nozzles are configured and aligned,

• - That quench water is injected only in the gas space, which is the downward flow encloses the raw hot gases withdrawn from the entrained-flow gasifier so that the raw gases deflected upward above the water surface are moistened and cooled before they interfere with the downward flow,
• That the surrounding walls of the quench space, but at least the surrounding walls of the gas space are cooled such that the temperature on the inner surface is 1 to 50 K below the dew point temperature of the gas space,
• - And that the quench space is dimensioned so that the mean residence time of the raw gas in the quenching chamber is 2 to 10 s.

To An advantageous embodiment of the invention is in the lower region the downside inflow the crude gases, the water bath superior Gas outlet for converted raw gases disposed having a Umlenkhaube.

Based 1 an embodiment of the invention will be explained in more detail.

1 shows a simplified schematic representation of an air flow gasifier downstream quench device with a raw gas inlet ( 2 ) to the downward inflow ( 9 ) hot raw gases ( 1 ) of the entrainment gasifier. The quenching room ( 4 ) consists of the gas space ( 5 ), the water bath ( 6 ) and is surrounded by perimeter walls ( 7 ) limited. The surrounding walls ( 7 ) of the quench space ( 4 ) are separated from the water jacket ( 18 ), in which saturated steam ( 19 ) is generated at a pressure of 10 bar. The converted crude gases ( 10 ) are via the gas outlet ( 20 ) deducted. The gas outlet ( 20 ) is with the deflection hood ( 21 ) to protect against entrainment of sprayed water. The lower part of the quenching chamber is a water bath ( 6 ) educated. In the gas space ( 5 ) range in several levels nozzles ( 14 . 15 . 16 ) for the introduction of quench water. The nozzles ( 14 ) and ( 15 ) are directed upwards. The nozzles ( 16 ) in the upper part of the gas space are in the direction of the raw gas inlet ( 2 ).

In the 1 shown quench device is used as follows:
The raw gases ( 1 ) of the entrained-flow gasification of lignite dust are from above by means of the raw gas inlet ( 2 ), the raw gas inlet ( 3 ) into the quench space ( 4 ) injected from the gas space ( 5 ), the water bath ( 6 ) and the surrounding walls ( 7 ) consists. The lower boundary of the gas space ( 5 ) is passed through the water surface ( 8th ) of the water bath ( 6 ) educated. The raw gases ( 1 ) enter the quenching chamber at a temperature of 1,450 ° C. and a pressure of 30 bar ( 4 ) one. The CO content of the raw gases ( 1 ) is 52.8% by volume (wet). As secondary components, liquid slag, some residual coke particulate matter and as volatile alkali compounds, chlorides and hydroxides of sodium and potassium are carried. The raw gases ( 1 ) are in the central zone of the downward flow ( 9 ) directed downwards. The conversion reaction takes place and converted raw gases ( 10 ). The converted crude gases ( 10 ) are at the water surface ( 8th ) of the water bath ( 6 ), whereby a part of the with the converted raw gases ( 10 ) entrained minor constituents in a water bath ( 6 ) and where they absorb water vapor. The converted crude gases ( 10 ) are then in the annular zone of the upward flow ( 11 ) led upwards and by means of the injected water ( 12 ) moistened. During the upward flow, the humidified, converted crude gases ( 13 ) increasingly with increasing altitude in the downflowing raw gases ( 1 ) one. The interference is in the 1 indicated by arrows. The volume flow of the upward flowing, humidified converted raw gases ( 13 ) is a multiple of the volume flow of the incoming raw gases ( 1 ). The water ( 12 ) is realized by means of three nozzle levels ( 14 ) 15 ) and ( 16 ), each consisting of six equally circumferentially arranged atomizing nozzles ( 17 ) exist, injected. The first nozzle level ( 14 ) is located just above the water surface ( 8th ), the second nozzle level ( 15 ) in the middle of the gas space ( 5 ) and the third nozzle level ( 16 ) at the upper end of the gas space ( 5 ). The first nozzle level ( 14 ) and the second nozzle level ( 15 ) spray upward and the third nozzle plane ( 16 ) inside. Per nozzle level ( 14 ) 15 ) and ( 16 ) are distributed evenly over all six atomizer nozzles ( 17 ), 0.166 kg of water ( 12 ) per kg of wet raw gases ( 1 ) is injected at a temperature of 200 ° C. The total amount of water injected is 0.5 kg / kg (raw gas, humid). The raw gases ( 1 ) during the downflow until reaching the water surface ( 8th ) to 700 ° C, which sets an approach temperature for the conversion reaction of 100 K. Accordingly, 44% of the crude gas ( 1 ) converted carbon monoxide CO by means of water vapor H ₂ O to carbon dioxide CO ₂ and hydrogen H ₂ . The gas space ( 5 ) leaving converted raw gases ( 10 ) have a CO content of only 18% by volume (moist). The high reaction conversion is due to the guidance of the flow and the effect of catalytically activated minor components, in which the entrained with the raw gases minor components by means of these raw gases during cooling in the central zone of the downward flow and during humidification in the annular zone of the upward flow with simultaneous enrichment the held in the gas space in suspension fixed and condensable secondary components are catalytically activated with the raw gases.

1

raw gases

2

Raw gas inlet

3

quench

4

Rohgaseintrittsmündung

5

headspace

6

water bath

7

containment

8th

water surface

9

headquarters Zone of downward flow

10

converted raw gases

11

Annular zone the upward flow

12

water

13

humidified converted raw gases

14

nozzle plane

15

nozzle plane

16

nozzle plane

17

atomizer

18

water jacket

19

saturated steam

20

gas outlet

21

deflection hood

Claims (11)

Process for the conversion of raw gases of the entrained flow gasification of carbonaceous feedstocks under pressure, wherein the withdrawn from a Flugstromvergaser hot raw gases are injected in a downward flow in a Quenchraum whose upper part is formed as a gas space and the lower part of a water bath, the lower limit of Gas space is formed by the water surface of the water bath, with quench water is injected and the raw gases are cooled and the raw gases are withdrawn above the water bath from the gas space, characterized in that - water is injected only in the gas space, which is the downward flow encloses the withdrawn from the entrained flow gasifier hot raw gases, so that the above the water surface upwardly deflected raw gases are moistened and cooled before they interfere in the downward flow, - that carried with the raw gases Neb enbestandteile be catalytically activated by means of these raw gases during cooling in the central zone of the downward flow and during the moistening and cooling in the annular zone of the upward flow with simultaneous enrichment of the gas space suspended in the supernatant solid and condensable minor components with the raw gases, and - Surrounding walls of the quench, but at least the surrounding walls of the gas space are cooled so that the temperature at the inner surface is 1 to 50 K below the dew point temperature of the gases of the gas space. Method according to claim 1, characterized in that that the water in at least one level or in several, over the Height of Gas space is distributed to distributed levels. Method according to claim 1 or 2, characterized that the water is injected as hot water, its temperature is at least 50 K below the boiling point and at the most at the boiling point at gasification pressure. Method according to one of claims 1 or 2, characterized that the water is called hot water injected whose temperature is at most 50 K above the boiling point at gasification pressure. Method according to one of claims 1 to 4, characterized that the perimeter walls the Quenchraumes indirectly cooled become. Method according to claim 5, characterized in that that for cooling Saturated steam is used at a pressure of 5 to 10 bar (abs.). Method according to one of claims 1 to 6, characterized that in the gas space so much water is injected that the leaving the gas space Crude gases temperatures in the range of 300 to 600 ° C have. Method according to one of claims 1 to 6, characterized that in the gas space so much water is injected that the leaving the gas space Crude gases have temperatures in the range of 600 to 900 ° C and given Values for the Sales of the conversion reaction can be adjusted. Method according to one of claims 1 to 8, characterized that the distance between the surface of the water bath and the inlet opening the raw gases in the gas space is reduced so much that the in the water bath evaporated amount of water at least partially takes over the function of the injected water and the amount of the injected Water is reduced accordingly. Device for the conversion of raw gases in the entrained flow gasification, consisting of a quench device downstream of an entrained flow gasifier with a raw gas inlet for downward flow hot exhaust gas of the entrained flow gasifier and a gas outlet for converted raw gases, wherein surrounding walls surround a quench, comprising a downwardly directed inflow of the hot raw gases Gas space and a water bath, characterized in that - at least in one plane of the gas space Extend nozzles for the introduction of quench water into the gas space and the nozzles are designed and aligned, - that quench water is injected only in the gas space, which encloses the downward flow of withdrawn from the entrained flow gasifier hot raw gases, so that above the water surface after above deflected raw gases are moistened and cooled before they interfere in the downward flow, and - that the walls surrounding the Quenchraumes, but at least the surrounding walls of the gas space are coolable so that the temperature at the inner surface 1 to 50 K below the Dew point temperature of the gases of the gas space is and that the quench chamber is dimensioned so that the mean residence time of the raw gas in the quenching chamber is 2 to 10 s. Device according to claim 10, characterized in that that at the bottom of the downside inflow the crude gases, the water bath superior Gas outlet for converted raw gases is arranged, which has a Umlenkhaube.