DE2312600A1 - THREE-STAGE GASIFICATION OF COAL - Google Patents

Description

Dlpl.-Ing. P. WIRTH Dr. V. SCHMIED-KOWARZIK Dlpl.-lng. G. DANNENBERG Dr. P. WEINHOLD Dr. D. GUDEL

281134 β FRANKFURT AM MAIN

TELEPHONE C0611)

287014 GR ESCHENHEIMER STRASSE 39

Wd / SK Case 4428

Bituminous Coal Research, Inc. 350 Hochberg Road
Monroewille, Pa, / USA

Three-stage gasification of coal

The present invention relates to the production of a with methane ■ Enriched fuel gas ("fuel gas") by gasifying coal in three stages at high pressures and temperatures.

Fuel gas enriched with methane is produced through a two-stage gasification process manufactured in which finely divided coal and steam in the second stage with synthesis gas from the first stage at one temperature above 870 C. and a pressure above 50 at to form charred material ("char") and a product gas containing hydrogen, methane and carbon oxides implemented. Charred material and product gas are withdrawn and separated, and the product gas is then treated to remove carbon oxides and other diluents and ultimately to form a methane-rich fuel gas methanated. The charred material is in the first gasification stage for reaction with water vapor and oxygen in one

Temperature above 1370 C. and a pressure above 50 at returned to a To form synthesis gas containing hydrogen and carbon oxides of the first stage for reaction in the second gasification stage. Part of the charred.

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Material that has a low sulfur content can be incinerated to produce process energy. The ones from the reactions of the first and second

because of their weight

Slag formed in the first stage sinks / in the first stage into the lower reactor section where it is cooled and removed from the procedure. Reaction times and residence times of the reactants in the first and second Stages are limited and kept to a minimum to prevent softening and agglomeration of the coal in the second stage.

The two-stage gasification process described above was developed by the Bituminous Coal Research, Inc., Pittsburgh, Pa., USA (BCR). That The procedure is described in a publication by the Ministry of the Interior, Office of Coal Research (OCR) published in 1965, entitled "Gas Generator Research and development, overview and evaluation ". In addition, this is Procedure in a computer study entitled "Computer study two-stage Reactions in the BCR two-stage overpressure gasification process "described, presented at the American Chemical Society National Meeting, Fuel Chemistry Department, Chicago, 111., September 1967.

The present invention resides in a process for the three-stage gasification of coal to form a methane-rich fuel gas. In the first stage, recirculated charred material is reacted at high temperature with oxygen and water vapor at a pressure of at least 5G at to form a synthesis gas containing hydrogen and carbon oxides of the first stage. In the second stage, the synthesis gas of the first stage is reacted with superheated steam and coal at high temperature and a pressure of at least 50 atm to form a product gas of the second stage which contains methane, hydrogen and carbon oxides. In the third step, the partially gasified char is maintained as a fluidized bed by the product gas of the second stage, the charred with the material

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forming a partially gasified char from the third Stage reacts in the product gas containing methane, hydrogen and carbon oxides the third stage is carried. Temperatures and residence times of the reactants in the first and second stage are controlled so that the ashes of the charred material in the first stage are converted into molten slag and the coal partially converted into methane, hydrogen and carbon oxides containing gas at temperatures above the plasticity range the coal is converted in the second stage. The temperature in the third stage is lower and the residence time of the solid reactants in the third stage longer than the first and second stages to get a more complete Allow exploitation of the reactants in the third stage. The third stage char and product gas are separated; and while the char is returned to the first stage for further reaction in the process, the third stage product gas becomes the conversion and removal of carbon oxides, hydrogen sulfide and other contaminants cleaned and then methanated to form a fuel gas with a methane content of at least 70%.

In one embodiment, the third stage and the fluidized bed of carbonized material are in direct communication with part of the second stage. In In another embodiment, the third stage is separate from the first and second stages. The slag formed in the first and second stages is collected in the lower part of the third stage and removed from this.

The gasification of the swirled in the product gas of a two-stage gasification process Charred material allows the partially gasified charred material to further react in the hydrogen-rich product gas of the second Stage at lower temperatures and longer residence times, resulting in a higher methane yield with greater carbon utilization at lower levels Oxygen requirements achieved.

3 0 9 8 U 2 I 0 Ί B 3

Figure 1 of the accompanying drawings is a diagrammatic representation an apparatus for carrying out the method according to the invention, in which the part of the gasification vessel for the third stage with that of the. second stage communicates.

Figure 2 is a diagrammatic representation of one used in the present invention Apparatus wherein the third stage is separate from the first and second stages "is.

Figure 3 is a diagrammatic representation of one used in the present invention Apparatus in which the third stage is separated from the first and second stages and a part of the char formed in the third stage is cooled and returned to the third stage.

Figure 4 is a diagrammatic representation of one used in the present invention Apparatus in which the third stage is separated from the first and second stages and the char separated from the second stage gas into the dr ± e stage and in this through a hydrogen-rich gas which is passed up through the third stage to form a fluidized bed.

In the present application, the term "coal" refers to anything carbonaceous material including all kinds of coal, lignite, etc.

The term "gasification" means heating coal in the presence reactive agent, eliminating all or part of the volatile fraction the coal is released and at least some of the carbon in the honest charred material with these reagents or with others, in the gasification process reaction participants present is implemented ".

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The term "product gas" means a methane-containing gas such as that in the third stage of the three-stage gasification process described above formed gas,

In the method illustrated in Fig. 1, a gasification vessel 10 comprises the First stage section 12; the section of the second stage 14 and the Third stage section 16. Recirculated partially gasified char is passed through line 18 to the first section 12 of the gasification vessel 10 led. Oxygen and water vapor are passed through line 20 to the section of the first stage 12 and there with the partially gasified Material are reacted as they flow down through the first section 12. This reaction produces a hydrogen, carbon oxides and other products including the molten slag formed from the ashes of the char - containing synthesis gas of the first stage.

In the section of the first stage 12 of the gasification vessel 10, the reaction takes place at a pressure of at least 50 at _7, preferably above 70 at. The temperature and residence time of the reactants in the first section 12 are set so that rapid gasification of the cooled material at a temperature above the Ash melting point of the charred material is guaranteed. A temperature of at least 1370 G. is preferred, and the residence time in the first process stage is preferably less than 2 seconds.

The first stage molten slag and synthesis gas flow downward through a mixing part or neck 22 in the gasification vessel 10, in which the velocity of the synthesis gas of the first stage and the slag, which flow into the upper part of the second section 14 is increased. money and water vapor are introduced through nozzles 24 into the upper portion 26 of the second stage portion 14 near the point where the

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Mixing part 22 in the second section 14 opens. The coal and steam nozzles 24 can also be in the mixing part 22 above the second section 14 open. The charging of coal and steam through nozzles 24 and the introduction of the first stage synthesis gas and molten slag the mixing part 22 ensures that these are mixed rapidly and thoroughly Reaction participants after entering the upper part 26 of the second Section 14, causing a rapid reaction of the coal with the synthesis gas the first stage and the water vapor as well as a fast transfer of a substantial amount of sensible heat from the molten slag to react Coal to be ensured / Due to the rapid "heat transfer from the molten slag to the bald, the former cools faster and solidifies before a noticeable accumulation of the molten slag can take place on the walls of the gasification vessel 10 in the second section 14.

This also enables the rapid heat transfer from the slag to the coal

re
a full / and more effective carbon utilization.

In the section of the second stage 14, the coal reacts with the water vapor and Synthesis gas of the first. Stage to form a second stage product; this includes partially gasified charred material contained in methane, hydrogen and carbon oxides-containing product gas of the second stage is entrained. The reaction of the second stage takes place at a pressure of at least 50 at, preferably above 70 at, and at such a temperature and ver- because time that a rapid reaction of the coal bsi a temperature above the area of plasticity is ensured. The temperature of the second

ο
Stage is preferably at least 870 ° C., while the residence time of the coal in the second stage is preferably less than 10 seconds, in particular less than 4 seconds.

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At the bottom of the second section 14, this runs in the product gas of the second stage entrained, partially gasified charred material through a deflection part 28 of the gasification vessel 10, which determines the direction of flow of the products of the second stage and directs it into the section of the third stage 16 which extends upwards around the second section 14 and partially dicises includes "

Due to the rapid cooling of the molten slag in the upper part; il

26 of the second section 14 and the further loss of heat through the downward slag flowing through the second section 14 solidifies it

by their weight with the formation of grains and larger particles, which sink through the entrained char and the product gas of the second stage and, due to their higher density and larger size, collect in the slag collecting section of the gasification vessel 10 within the third section 16 below the deflection part 28. The slag collected in section 3U runs downwards through a conduit 32 into a slurry section 34 ("elutriation portion") in the gasification vessel 10, where the slag is slurried with water vapor in order to remove the lighter particles of the partially gasified, trapped in the slag collecting section 30 in the slag, The slurried char runs up with a portion of the slurry water vapor into the third section Ib .

The heavier slag particles run with part of the Aufschlärnrr.wasser— steam down through line 36 into slag quenching section 36, where the slag is quenched with water and finally as cold slag is removed from the process by line 40.

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The dimensions of the portion of the third stage 16 are selected so that charred material and product gas of the second stage in the third section 16, which partially encloses the section 14, form a fluidized bed. The linear gas velocities in the third section 16 are adjusted so that they ensure the formation of the desired fluidized bed; they are expediently in the third section 16 between about 0.15-6 m / sec, preferably between 0.3-3 m / sec.

The reaction in the third stage of the process takes place near the pressure the second stage. The temperature in the third stage is lower than that of the second stage, and the residence time of the char in the third stage is much longer than the first and second stage of the procedure. The temperature of the third stage is expediently about 815-9DD C. The residence time of the charred material in the third Level should be at least 5 times, preferably 20 times or more,. the residence time of the product gas of the second stage and other gases there

wear. A residence time of the char in the third stage of 20 minutes or more is preferred, especially if high quality charcoal is used.

("elutriation")

The slurry / 'from the reaction of carbon with hydrogen to form methane shows higher methane yields for lower temperatures. Therefore, the reaction in the third stage results in a lower temperature than in the second stage with a longer residence and reaction time in the presence a larger amount of charred material and a larger volume of the hydrogen-rich product gas contained in the third stage higher gasification rate and higher methane yield with lower oxygen requirements than in the two-stage gasification process.

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Some of the products from the third gasification stage are gasified, in the methane, hydrogen and carbon oxide-containing product gas of the third Stage entrained char through line 42 in a separator, e.g. a cyclone separator, where the partially gasified charred material is separated from the product gas of the third stage. That charred Material is fed through line 46 to a water dip pan 48, where it is mixed with water vapor at slightly higher pressure than that in the first gasification stage. Charred material and water vapor become returned through line 18 to first section 12 for further reaction in the process.

The separated product gas of the third stage is withdrawn through line 50 and passed to a cleaning device 52, where it is converted and Removal of carbon oxides, hydrogen sulfide and other contaminants. The purified product gas of the third stage runs through Line 54 to the methanation device 56, in which it methanates catalytically and through line 58 as fuel gas with a methane content of at least about 70 vol .- ^ i, preferably at least 90 vol .- ^ 4, is removed.

In the method illustrated in FIG. 2, certain modifications of the method according to the invention shown. Partially gassed, 'returned, Charred material mixed with steam is fed through line 60 into a first gasification section 62 of a two-stage gasification vessel 64 introduced. Oxygen and water vapor are in the first through line 66 Section 62 introduced and reacted there with the charred material to form synthesis gas of the first stage.

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In the process shown in FIG. 2, there is no passage of the synthesis gas of the first stage or other reaction products of the first stage through the mixing part or throat as in the procedure of Example 1. Instead, run Synthesis gas and other reaction products from the first stage directly into the upper part 68 of the second gasification section 70, where a rapid and intimate mixing of synthesis gas and other reaction products of the first Stage by introducing coal and superheated steam through the nozzles 72 takes place, which are controlled so that the necessary reactant speeds and achieved appropriate direction for the desired mixing and rapid heat transfer. Reaction temperatures, pressures and Residence times of the first and second stages are practically the same as described for the process shown in FIG.

In the method of FIG. 2, a third gasification section 74 is provided which is kept separate from the first and second sections 62 and 70, respectively. Partially gasified second stage char, entrained with the methane, hydrogen and carbon oxides-containing product gas of the second stage, is passed through line 76 to the lower portion 76 of the third section 74 where the second stage char through the hydrogen-rich product gas of the second stage is kept vortexed. The temperature, pressure and residence times in the third stage are practically the same as those given for the third stage of the process illustrated in FIG. It should be noted, however, that the process of FIG Section of the second stage 70 to the fluidized bed of the carbonized material in the section of the third stage 74 prevents the temperature, particularly in the upper part of the fluidized bed of carbonized

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Material in the third section 74, and thus increase the methane yield the reaction of carbon with hydrogen.

In the process of Fig. 2, slag is produced by the second stage product gas and entrained char through line 76 for collection in the lower Part 78 of the third section 74 transported. Slurrying, quenching and removal of the slag from the third section 74 occurs in the above for the method of Fig. 1 described manner. In the following, ver- Driving elements that are identical to process elements in embodiments and drawings already described are given identical reference numerals referred to as they were already used in previous embodiments and drawings.

The removal of the char and product gas from the third Stage including its subsequent return, cleaning, etc. Methanation takes place as in the process of FIG gaseous hydrogen sulfide removed from the product gas of the third stage withdrawn through line 80 and reacted in the sulfur recovery reactor, e.g., a CDaus reactor, 82 to form elemental sulfur will.

In the method illustrated in FIG. 3, the stages are the first and last second gasification identical to the process steps of Fig. 2 with the exception, that the char and the water vapor returned to the first stage have a slightly different composition, as follows will be explained in more detail.

The product gas introduced into the third section 74 through line 76 second stage and the charred material becomes formation in the third stage converted by partially gasified charred material, that in methane,

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Hydrogen and carbon oxides-containing product gas of the third stage is entrained during, the collection, slurrying and removal of the Slag from the third section 74 take place in the manner described above.

In the process of FIG. 3, the charred material of the third stage and the Third stage product gas withdrawn from third section 74 through line 82 and quenched with water or other flowable suitable material and sent to a primary separator 84. The separator 84 separates the product gas of the third stage, water vapor and the fine charred material entrained therein from the coarser, heavier particles of the charred Material from the "third stage, the cooled coarser charred material is passed through line 86 to steam device 88. Steam and coarse charred material is passed through line 90 into the lower Part 78 of the third section 74 introduced for further temperature control of reactants at this stage to enable and additional Carbon or other reactants in the char for to create the third stage response. The repatriation of further quantities of charred material at low temperatures to the third section 74 results in a further increase in methane yield and carbon utilization with low oxygen requirements.

The product gas of the third stage and the fine, in the primary, carried along with it Charred material separated from separators 84 is withdrawn through line 92 and passed to a secondary separator 94 in which the separating fine char from the third stage product gas; the latter is through line 96 for cleaning and methanation with production of elemental sulfur in the manner described in the process of FIG. The separated, withdrawn from the secondary separator 94, fine charred material is passed through line 98 to a steam device

309842 '/ 0383'

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100 passed to as a mixture of water vapor and charred material a pressure higher than that in the first stage through line 102 to be returned. . -

In the process shown in FIG. 4, charred residues are recycled Material and water vapor introduced into the first gasification stage 106 portion of a gasification vessel 106 through line 104. Water vapor and Oxygen is introduced into the first section 106 through line 110 and flows up through it with recirculated char Section of the second gasification stage 112. The reaction conditions in the first and second stages are similar to the others, already described Process with the exception that the flow through the first and second gasification stages takes place in the ascending direction and a mixture of coal and water vapor through line 114 in the second section 112 above the first section 106 is introduced to be entrained in the synthesis gas of the first stage and other products of the first stage when these up flow into the second section 112.

Molten slag arising from the ashes of the first and second stages formed charred material accumulates on the walls of the first and second sections 106 and 112 of the gasification vessel 108. The accumulated molten slag sinks to the lower part 116 of the first Section 106 from where it collects and through line 118 to the subsequent Quenching and removal from the system is performed.

The product gas of the second stage with entrained charred material is removed through line 120 and to a primary char Material 122 out. In the separator 122, the fine charred material of the second stage mixed with the product gas of the second stage is separated off and removed from the coarse-carbonized material passing through line 124 to the upper

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Part 126 of the third gasification section 128 is passed. While As the coarse charred material moves down through the third section 128, a hydrogen rich gas is passed through line 130 to the lower portion 132 of the third section 128 and runs up through the third section 128 to form a fluidized bed with the downward moving coarse char. The method of Figure 4 enables use a third section 128 of smaller size than gasification vessel 1G8, Since the swirling with hydrogen or a flowable gas enriched with hydrogen, higher methane yields with lower volumes of swirling Gas allows.

The hydrogen-rich gas is before introduction into the third stage on a Print at least 7? Atü compresses and holds the sinking coarse charred Material in a fluidized bed. When the sinking coarse charred material reaches the point of introduction of the hydrogen-rich gas at the lower part 146 has passed, it enters a slurry section 134 in which the hydrogen-rich gas by a slurrying flowable. Material like Water vapor, is replaced. Some particles of the carbonized material are lifted up out of the blowdown section by the slurrying water vapor carried and returned to the third stage reaction.

The remaining particles of the char slurried in the slurry section 134 Material pass down through line 136 to a steam device 138. A mixture of water vapor and char is then passed through line 104 as described above to the. First stage section 106 returned.

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The second stage product gas removed from the primary separator 122 entrained fine char is passed through line 138 and quenched with water for introduction into secondary separator 140. The third stage product gas with entrained char is passed through line 142 from top 126 of third section 126 and mixes with the quenched char in line 138 and second stage product gas from primary separator 122 for introduction into secondary separator 140.

In the secondary separator 140, the product gases from the second and third stage separated from the charred material of the second and third stage. The separated char becomes one through line 144 Intermediate portion 146 of slurry section 134 to mix with the coarse slurry char in slurry section 134. The mixture of coarse slurried and fine charred material Separator 140 in slurry section 134 is through line 136 into the Steam device 138 introduced and at a pressure above that in the the pressure prevailing in the first gasification stage. The resulting mixture of char and introduced water vapor is passed through line 104 returned to the first section 106 for further reaction in the process.

Mix of

The / in the secondary separation device 140 separated product gases of the second and third stage is through line 148 to a cleaning device 150 in which the gases are passed through a water gas rearrangement reactor and hydrogen sulfide and carbon dioxide are removed as separate streams. The gaseous hydrogen sulfide is converted into a sulfur through line 152 conversion reactor 154, e.g. a Claus reactor, for conversion into elemental sulfur.

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9 Q 1 9 ο η ρ) - 16 - ■ '

Some of the purified product gases can pass through lines 156 and 15Θ to a compressor 160 and further through line 130 to the section of the third Stage 128 are performed while the remaining cleaned. Product gases are passed through line 162 to methanation device 164. Part of the cleaned Product gases can also be passed through line 156 to a hydrogen separator 168, which can be a cryogenic separator, .in-which hydrogen or a hydrogen-rich gas is separated and through Line 170 is withdrawn and passed to the compressor 160, to then through the line 130 for the hydrogen-enriched gas at a higher pressure than the pressure in the third stage, preferably about 77 atmospheres, to the third gasification section 128 to be returned.

many
As shown in FIG. 4, there are / are possible modifications to the ultimate use of the purified product gas transported through line 156. The the Wasserstoffabtrennvorrichtung 168 leaving, purified product gas is passed through line 172 to the Methanierungsvorrichung 164, where it is catalytically methanated to form fuel gas or fuel gas having a methane content of at least 70 vol .-%, preferably about 90 vol jo.

An unplanned or undesirable temperature increase in the third stage is prevented by the water vapor entering the third section 128 from the slurry section 134 as the evaporated water is in the third Step entering water vapor reacts endothermically with carbon to form carbon monoxide plus gaseous hydrogen.

The process according to the invention can be used for production with certain modifications used by generator gas from the three-stage, gasification of coal will. In the production of generator gas, the first gasification 2nd stage introduced combination of oxygen and water vapor through air

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231/600

replaced as a gasification medium. The air should be around 480-705 C. or more be preheated. The air is introduced into the first gasification stage to react with the recycled char. The reaction pressures in the three separate levels should be kept between about 5-6Ü at. The remaining reaction conditions and process steps have already been mentioned above described. The generator gas obtained by this process using preheated air as the first stage gasification medium, is particularly suitable as an industrial fuel or as a fuel for power generation, in which the release of sulfur dioxide is undesirable.

The advantages of using the three-stage gasification process according to the invention in comparison to a two-stage gasification process, by comparing the following tabular calculations of the composition of fuel gases from each process and by calculating the possible coal and oxygen requirements for each process.

Table 1

according to the invention 2-stage 3-stage process Process

Gas analysis from the carburetor;
Dry basis

Vol .- "/" CH ₄ 28.2 20.5

H ₂ 17.9 "24.1

CO 27.5 34.4

CO ₂ , H ₂ S 24.8 19.6

N ₂ 1.6 1.4

For 26.3 m (standard condition) pipeline gas are required:

Money; kg 40.14 41.96

Oxygen; kg 13.02 16.87

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Claims (1)

Claims £ O \ /. OUU 1.- A method for the gasification of coal, characterized in that one partially gasified,. recycled charred material in a first gasification zone introduces, introduces oxygen and water vapor into this first gasification zone, Oxygen and water vapor with the partially gasified, recycled char material to form one comprising hydrogen and carbon oxides Converts synthesis gas of the first zone and slag formed from the molten ash of the partially gasified charred material, the synthesis gas of the first zone and the slag in a second gasification zone introduces,. Coal, steam, synthesis gas in the first zone and slag in the second Gasification zone to form a product of the second zone converts that Carries a partially gasified char and sfethane, hydrogen and includes carbon oxides, the product gas from the second zone, and since s te ilweise gasified char the second zone in a third gasification zone is introduced, in the third gasification zone a fluidized bed from which is partially gasified charred material of the second zone in a swirling stream of the product gas of the second zone, the partially gasified char of the second zone in the third Gasification zone with the product gas of the second zone to form a partial gasified charred material of the third zone converts that in the Third zone product gas comprising methane, hydrogen and carbon oxides is carried, 3098A2 / 0363 the partially gasified char entrained in the product gas of the third zone Material removed from the third gasification zone, the partially gasified char of the third zone from the product gas separates the third zone, the partially gasified charred material with water vapor to form the mixed partially gasified charred material to be returned, the partially gasified char recycle material to the first gasification zone returns, that separated from the partially gasified char in the third zone Third zone product gas for removing carbon dioxide, hydrogen sulfide and other impurities and receives a purified product gas of the third zone and the latter methanated to form a fuel gas containing at least 70 vol. 2.- The method according to claim 1, characterized in that one the reaction in the third gasification zone at a temperature between about 815-B70 ° C. performs. 3.- The method according to claim 1 and 2, characterized in that one for the partially gasified char of the second zone in the third Gasification zone maintains a residence time that is at least 5 times the residence time of the product gas of the second zone in the third gasification zone. 309842/0363 . ■ "■" ^m ~ ' 2312800 4, β · method according to claims 1 to 3 _? dadyreh geKennzeieH.net that the synthesis gas of the first Zp.ne. and gchlacke from the first \ /§rg§.sungsz; i3n§ vpr their introduction? in the second gasification zone d.yr§h §in§ MiSS-hzine leads ι to a fast mixing ynti ftea.gierBn between coal ,? §Yn.th.es, iga§ of the- first zone, and water vapor to ensure ynd a, getinslle V ^ iFfflg = transfer from the slag of the first ye.rgasMngs, zpne zyr Kshlg §ishgf zy = places,. -§, - * ■ Method according to claim 1, part 4, da ^ yrgh Oxygen, water vapor and partly yergaste§, zyryekg@fü.h.rtg§ material downwards dyrEh the er ^ te V§ ¥ "i8sungszsn§ fefe.weft _f S.ynthe§egas of the first zone, slag, throat ynd Was.serdam.pf && W8rts the second gasification zone moves ynd partially gasified, chilled material from the second zone. the second zone up through the third gasification zone ß. «Method according to claim 5, characterized in that it is marked, dgiß m.a.n dig chopped with charcoal in the second gasification process, and mixes between two heats from the cloth to the charcoal. Φ in the second V ^B .rga§yng§zgne a solidified j finely divided gchlaelsg forms, the solidified, finely divided. §E.hlaek-e and e, in §n part d§§ partially vgr « gasten yerkohiten material of the second Zope in the lower) section of the third gasification zone collects, ".-., - the solidified, finely divided? Slag ynd the partially ye.rgaste yerkihlP Materia.1 of the second zone ays of the third Ve.rgasyn.gszpne in 30IS42 / 03 the solidified, finely divided slag and the partially gasified slag Material of the second zone in contact with silting water vapor brings, part of the slurrying water vapor with the entrained, partially gasified charred material of the second zone is returned to the third gasification zone for reaction and quenched the solidified, finely divided slag after slurrying. ,? .- Process according to Claims 1 to G, characterized in that the second gasification zone at least partially from the third gasification zone includes and the partially gasified charred material of the second zone, the product gas the second zone and the slag directly from the second gasification zone in introduces part of the third gasification zone. 8.- The method according to claim 1 to 7, characterized in that one the third zone product gas and the partially gasified char mixing the third zone with water to cool the partially gasified charred material of the third zone, the partially gasified char of the third zone that is in the product gas the third zone is carried into a coarser and a lighter, separates fine fraction, the coarser portion of the partially gasified charred material of the third Mixing tongue with steam, the coarser part of the partially gasified material of the third zone with Returns water vapor to the third gasification zone, the lighter portion of the partially gasified charred material of the third Zone separates from the product gas of the third zone, 309842/0363 the lighter portion of the partially gasified charred material of the third zone mixes with water vapor and returns it to the first gasification zone with steam. The patent attorney: 30984 2/0363 empty «