DE1058193B - Method and device for generating water gas in two gasification shafts - Google Patents

Description

The production of water gas for chemical-industrial and other purposes after the periodic With the current state of the art, the bubble-gas principle is subject to various requirements and restrictions bound, which aggravate and make more expensive.

It is well known that shaft gas generators charged with coke or non-baking coal are operated in this way that you alternately blow hot with air and gas with steam. It burns when hot-blown Oxygen of the blowing wind - forming blowing gas - in the coke column of the gas generator, this around a certain Heat amount heating up. The storage heat is generated by the subsequent gases heat-binding reaction of the formation of water gas is consumed again. The smaller with a certain the required throughput of the gas generator is the amount of heat stored during hot blowing, the more The individual gas periods become shorter and more numerous, and the more water gas is lost as purging lost when the system is moved frequently.

During the blowing process, due to the chemical processes taking place and the laws of heat transfer, a temperature distribution over the height of the coke column which is in reaction can only be influenced to a very limited extent. The aim must be to achieve the highest possible temperature in all parts of the coke column by blowing, since then both the storage heat increases and extensive water vapor conversion takes place in the subsequent gases, which increases the throughput and gasification efficiency of the system. The reactions of the formation of water gas are in fact highly temperature-dependent with regard to their expiry speed; in particular the process preferred and desired in terms of equilibrium due to high temperature: C + H ₂ O = CO + H ₂ . Its reaction rate increases in the range from 800 to 1500 ° C per 100 ° C increase in temperature on average 2.8 times.

However, up to now one has been limited to the use of relatively low gasification temperatures, on the one hand because the ash melting point in the commonly used rotary grate gas generators is not may be exceeded, and secondly, especially for the following reason:

As is well known, the atmospheric oxygen of the blowing wind initially burns completely to carbon dioxide in the lowest gasification zone and is then partially converted to carbon monoxide _{on the hot coke surface according to the reaction equation C + CO 2 = 2CO.} Here again around 1800 kcal per Nm ³ converted CO ₂ of heat are consumed.

Method and device

for the generation of water gas

in two gassing shafts

Applicant:

Dr.-Ing. Friedrich Johswich,
Essen-Süd, Schubertstr. 45

Dr.-Ing. Friedrich. Johswich, Essen-Süd,
has been named as the inventor

needs, which is lost as storage heat and appears as undesirable chemically bound heat in the blown gas, which can practically only be used to generate gas vapor. The CO formation or CO ₂ conversion increases with temperature even more than the water vapor conversion; their speed increases approximately 3.7 times for every 100 ° C. The hot blowing can therefore only be carried out for a relatively short time because the temperatures increase in the lower part of the gas generator and ultimately lead to the CO content in the blowing gas exceeding the economic limit. With an increase of the CO content in the gas bubble 1% each of A ^ is ergasungswirkungsgrad namely about 2 ° / o lowered. According to the Dellwik-Fleischer process, efforts are made to reduce this disadvantage by using high blowing speeds. At today's high wind speeds of around 8000 Nm ^s / h per m ^{2 of} empty shaft cross-section, the CO _{2 is} only given a fraction of a second (0.05 to 0.1 seconds) to decompose and also the zone where the oxygen is burned to CO ₂ pulled apart in height, which compensates for the maximum temperatures occurring there.

Nevertheless, one cannot avoid a compromise on the question of the gasification temperature and must be satisfied with it, gasification efficiencies not above 65%, water vapor conversion rates not more than 50% and CO contents in the blow gas not to be reached under 6 * / ».

In addition, the extremely high blowing speed places considerable quality requirements on the gas to be gasified Fuel, which must be coarse, well classified and dimensionally stable in the fire so that it can be used

909 E-2S / 1S »

the gas flow is not carried out of the gas generator and the flow resistance is not too high caused.

The following, operationally, also contributes to the rather poor degree of water vapor conversion conditional circumstance in:

Disregarding the very brief period of backward gassing, there is both blowing and gassed from bottom to top. At the end of the bubbling period there is one in the lowest gasification zone Temperature from 1100 to 1300 ° C, which first drops quickly upwards, then more slowly to about 400 ° C at the blower gas outlet. Temperatures below 800 ° C are due to the then slow reaction rate not very effective with regard to the conversion of water vapor and result in only very little under the prevailing operating conditions Sales. In terms of performance, therefore, only the formation of water gas in the lower, particularly hot ones, is significant Zones of the gas generator. Here, however, the one reached under the victim of the CO formation during blowing high temperature after the start of the gassing quickly lowered by the impacting cold water vapor, which can only react in the sense of the formation of water gas when it is appropriately heated. In terms of numbers, this has the following effect:

Assuming that initially a sufficiently extensive temperature zone in the gas generator lower part of 1200 ° C in order to enable a 75% conversion of steam supplied at the same temperature, the following comparison results:

In order to convert 1200 ° C hot steam to 75 <> / », 0.75 2500 = 1880 kcal per Nm ^{3 of} gas vapor are consumed and the temperature is constantly reduced depending on the height of the hot coke layer and the steam exposure.

In order to first heat the same steam to 1200 ° C and then convert it to 75%, (1200-150) 0.42 = 440 kcal more or a total of 2320 kcal per Nm ^{3 of} water vapor must be used, ie the efficiency of the high temperature zone decreases by 20 per cent. Of course, this value is only an estimate of the order of magnitude, and one more serious circumstance must also be taken into account, the calculation of which is too complicated to be reproduced here: The high reaction rate prevailing at 1200 ° C is of course only fully reached when the steam is preheated to this temperature. Until then it has to flow through a considerable part of the reaction layer, and its residence time at 1200 ° C. is thereby considerably shortened, so that a conversion of 75% is no longer achieved in any case.

As can be seen, it would be much more advantageous to gas from top to bottom and the gas at the top Coke layers at a lower and therefore less effective temperature for preheating in terms of gasification technology to take advantage of the steam. With the gasification plants according to the previous state of the art this is not possible because the water gas then has an uneconomically high outlet temperature from the Gas generator and the rotating grate would not be able to withstand such stress.

The previous type of blowing and gassing thus leads to the fact that when blowing is in the gas generator lower part forms a relatively narrow temperature peak, which leads to harmful CO formation. These for the water vapor conversion, in turn, the extremely favorable temperature peak cannot be fully exploited because it is broken down too quickly when gassing. Your heat content is formed by the below Water gas and the remaining water vapor carried up and quickly leveling the temperature of the whole coke column, with the water vapor conversion increasing at the top, but not removed to the extent that it thereby decreases below. After all, those in the course of the gassing are also on top reached temperatures cannot be fully exploited, as the

ίο gases must be interrupted as soon as the constant inflow of cold steam in the lower part of the gas generator, the ignition temperature of 600 to 700 ° C threatens to be undercut.

The stated disadvantages of the previous processes have led to the need for chemical synthesis plants and other large-scale consumers today almost exclusively gasification plants after those with oxygen-water vapor mixtures can be built as an underwind continuously working process, although they are due to the necessity of additional Construction of air separation plants are much more expensive. There was therefore an incentive given to one Developing water-gas processes based on the bubble-gas principle, which is probably the relatively low one Investment costs, but not the acceptance of the previous disadvantages and application limits; especially for gas works and other smaller units. So the task at hand was to do the Bubbles generate a storage heat of practically any size at a high temperature without affecting the C O content of the blow gas exceeds the economically permissible limit. Furthermore, when gassing, the high Temperature can be used to the greatest possible extent and still use both bubble gas and water gas Leave the gas generator at low temperatures not exceeding 500 ° C. To have general applicability to ensure the process, it must not be based solely on metallurgical coke, Anthracite and similar high-quality fuels must be limited, but must also be used extensively any coarse or fine grain solid fuel including bituminous coals as well liquid or gaseous fuels of all kinds.

The invention enables this. It is based on an arrangement in which two gassing shafts are provided, the tops of which are connected to one another via a heat accumulator and which are switched one after the other when the gas is gassing. The invention proposes in such Set up the two gasification shafts also during the changing order of the gasification shafts and to connect in the opposite direction blowing over the heat accumulator one behind the other and the blowing wind and / or the gas vapor in a manner known in the case of water gas generators working according to a different principle partly below the fuel bed of one shaft, partly above the fuel bed of one or feed both shafts.

There is already a method known in which two gasification shafts both when blowing and when Gases are connected in series. Here, however, there is a lack of heat storage, which leads to the following disadvantage leads.

When using the bubble gas process with two gasification chambers If the highest possible degree of water vapor decomposition is to be achieved, then it must Hot blowing the first fuel bed can be driven very high. But this increases the CO content

I 058 193

the bubble gases are relatively high. The combustion of the same gives a large amount of heat, which in the second fuel bed would lead to renewed formation of CO. That is when the invention Process countered by the heat accumulator. The second fuel bed is avoided in this case from new CO formation only heated up to such an extent that it is still in it during the subsequent gassing a large part of the undecomposed water vapor which has passed through the first bed is converted.

The drawing shows an arrangement for carrying out the method according to the invention.

With 1 and 2, the gasification shafts and 3 with the heat accumulator are designated. The heat storage can be constructed according to the well-known Cowper system or of some other suitable form be.

4 and 5 are the top stoppers for the fuel feed because of the high internal temperatures the shafts are expediently cooled in any known form.

The fuel bed rests in each shaft either on a rotating grate or on the fireproof masonry the shafts, which are then conical at the bottom. There can be crushers for larger ones Lumps of slag are provided, or the rotating grate can be set up accordingly. Apart from Locks or water bowls can also use other discharge devices for the slag will. At 6 and 7 only simple slides are indicated. The contained in the discharged slag, unburned fuel components can be separated out and given back to the gas generator will.

8 to 11 are feed lines for the gasification means, namely wind blowing and gas vapor, their inventive Usage is explained below. With the help of the connecting pieces 12 and 13 are the Gas generator upper parts connected to the heat accumulator.

At 14 and 15, the outlet lines for bubble gas and water gas are indicated; at an operational They are arranged in such a way that the gases are drawn evenly across the gas generator cross-section and the passage of fuel or slag into the gas pipes does not occur. at If there is a rotating grate, the lines go off below it.

The gasification shafts are at the points where, in addition to the temperature stress, they are also more mechanical Wear of the refractory internal masonry by the fuel is added, expediently with Surrounding cooling jackets that are filled with water or through which steam or air flows. The latter can also be used advantageously for a certain preheating of the gasification means by you can pass this through the cooling jacket beforehand. For this purpose, the cooling jacket can also be attached to the upper parts of the gas generator and to be extended to the heat accumulator, which reduces the wall losses of the gas generator decreased. The heat dissipated from the outer wall of the gas generator and heat accumulator, the sensible heat of the water gas and / or the blown gas and the chemically bound heat of the The latter can be used in a known manner, in addition to preheating the gasification agent for generating steam or other thermal engineering purposes.

With the device described, the • according to the invention Procedure exercised as follows:

First, one of the shafts is first blown hot

and then gasified, the gasifying means, namely the wind blow and the gas vapor or the The bubble gas formed therefrom and the water gas flow upwards here. After the hot gases pass the Once the heat accumulator has passed, they flow through the second shaft in a downward direction and leave the gas generator below its fuel bed.

After one or more complete periods of gasification - consisting of bubbles and gases - the mode of operation of the two shafts is reversed, i.e. H. now from the other Manhole blown and gasified. This process is repeated in constant sequence, and in detail when blowing and gassing worked like this:

In the case of hot blowing, according to the invention, only a partial amount of the total blowing wind is supplied under the fuel bed of the first shaft - for example at 8. The other part occurs above the fuel bed - for example at 10. In one type of application of the method according to the invention, it is dimensioned so large that it is sufficient to completely burn the blowing gas formed in the fuel bed from the wind given below, its temperature increasing - especially towards the end of blowing - ■ greatly. A large part of the heat content of the flue gas generated in this way in the upper part of the first gas generator is collected in the heat accumulator, and the gas passes into the second gas generator, substantially cooled. It partially heats the fuel bed again, which had been almost completely cooled down by the previous gassing. As a result of the low temperature, there is hardly any _{conversion of CO 2} to CO, and the CO content of the blown gas remains below 1% on average. When blowing, the second fuel bed acts primarily as a downstream heat store, and the blowing gas leaves the gas generator at a very low temperature.

If the heat accumulator is adequately dimensioned, the temperature can be set when blowing of the first fuel bed drift up almost over its entire extent and especially here Create favorable conditions for the subsequent formation of water gas, without a substantial one Having to accept CO content in the blower gas. The type of procedure described requires that during the blowing process the proportion between the Uhterwind and the upperwind is in favor of the upper wind is changed, according to the time or the fuel bed temperature increasing C O content of the primarily resulting blown gas.

However, it is also possible, and often very economical, to save high-quality fuel Start by choosing a large and constant amount of upper wind while blowing. then becomes even finer-grained, more fluid, especially in the first part of the blowing above the fuel bed or other gaseous fuel supplied, in an amount as required by the oxygen excess of the upper wind can be completely burned. The heat generated during blowing then becomes more of the Heat storage shifted out, but it can od up to 15% of high quality coke Replace auxiliary fuel.

As mentioned, the heat accumulator has to absorb large amounts of heat - up to 2.0 · 10 ⁶ kcal - in the short bubble time. It cannot be made switchable to simplify operation

and to reliably avoid malfunctions in a switching device operating at up to 1600 ° C. Around To be able to build the heat storage tank smaller, one is also able to use a switchover flap or a To provide a similar aid, which does not need to close very tightly and allows the direction of flow reverse in memory each time after blowing. Then its hot end is with blowing in each case on the first gasification shaft and in the case of gassing on the second, whereby the storage and depletion takes place in the thermally most expedient direction.

If you have to gasify a fuel with a low ash melting point, you can avoid the downwind in some way - for example, as is known, by saturation - water vapor or carbon dioxide mix in. The first fuel bed is heated via the same high altitude, but to a lower maximum temperature than dry wind and avoids Difficulties in removing slag. The upper wind is still used dry, but must be dosed correspondingly higher in order to now also produce CO and hydrogen burn. Instead of air, another cheap, oxygen-containing wind can also be used as an upper wind standing gas, for example purge gas from an air separation plant, can be used.

In the case of gassing, according to the method according to the invention, either the entire or also only some of the gas vapor is introduced below the first fuel bed. The addition of the other part usually takes place in front of the heat storage tank, depending on the operational requirements, but in special cases partly or entirely behind the same.

At the start of gassing, the amount of sub-vapor can be selected to be large in any case, since the first The fuel bed is still very hot from the point of view of blowing and an extensive conversion of water vapor - up to 90 ° / o - enabled. The water gas, which has been somewhat cooled down by the upper steam, is absorbed in the heat accumulator high temperature and heats the second fuel bed, which is already preheated when blowing was continued, especially in the upper layers. Here the water vapor conversion is initially low, which is why there is no point in giving a lot of steam at the beginning. With advancing However, the water vapor conversion also rises up to 90 * / »at times during heating it constantly decreases in the first fuel bed as a result of increasing cooling. In the last part of the gassing the first fuel bed only serves to preheat the sub-steam and is finally up to cooled almost to the inlet temperature of the steam. This results in the fuel beds a large temperature range and a correspondingly high storage capacity for bubble heat or a low outlet temperature for bubble and water gas.

After the heat stored in the heat accumulator has also been used up, the second fuel bed has been set up likewise cooled down again from above to such an extent that sufficient water gas formation is no longer possible he follows. At the bottom, its temperature is now 600 due to the heat transfer from above has risen to 700 ° C, and the water gas emerging from the gas generator eventually becomes too hot. That Gassing is then stopped and blowing is started again from the second duct, whereby its fuel bed, as just mentioned, is already preheated to the ignition temperature during gassing became.

In order to make good use of the heat content of the storage tank, the top steam is usually conducted in front of it, so in the upper part of the first gas generator. But there are also cases in which it is better to use it completely or partially to be introduced only in the upper part of the second gas generator; namely when highly bituminous resp. Hydrocarbon-like additional fuels with gasified

ίο be a particularly powerful water gas accrues, as desired in gas works, for example. These additional fuels, such as coal dust, tar, Heating oil or the like, are then only added in the upper part of the second gas generator and above or gasified on the second fuel bed. The cold top steam added last here then protects the hot, heavy hydrocarbons before decomposition due to the high temperature of the heat accumulator or the gases leaving it.

If you are aiming for a high CO content in the water gas, you can use carbon dioxide alone or in a mixture with water vapor instead of pure water vapor as gas vapor. It is also sometimes advantageous _{to supply only CO 2} under the fuel bed and only water vapor above it. At a high temperature, the CO ₂ is converted more quickly than water vapor and causes the first fuel bed to cool down more quickly, which is sometimes advantageous when using a relatively large amount of top steam as described above. In addition, the hydrocarbons formed first from the additional fuels usually only split in the desired direction when there is water vapor in the gas space, but little or no CO ₂ at all. The top steam must then consist of pure water vapor and any required CO ₂ must be supplied under the fuel bed.

The main advantage of the method according to the invention described so far, namely his high heat economy, is shown below using a simple example of the gasification of metallurgical coke shown.

example

The gas generator consists of two shafts, each with an inner diameter of 3 m and a clearance height of 5 m. Each Fuel bed with a total height of about 3 m weighs about 101 and consists in its lowest part from slag. The heat accumulator has a diameter of 3.5 m and is 8 m high. It is not switchable. The shafts are equipped with rotating grids.

The blowing speed is 55,000 Nm ³ / h and the blowing time is 3.8 minutes.

The gas velocity is 14,500 Nm ³ / k or 11.7 t / li, and the gas duration is 8.2 minutes. There are therefore five complete gassing periods per hour. The gasifying agents are not preheated.

The water gas accumulation is at an average water vapor reacting 7O ° / o for each period 3250Nm ³ per hour or 16,250 Nm. ³ The calorific value is 2504 kcal / Nm ³ , the heat of combustion is 2736 kcal / Nm ³ . The average outlet temperature of the water gas from the gasifier is about 400 ⁰ C.

Fall to gas bubble per period 2930 Nm ³ per hour and 14650Nm ³ with an average Co content of Ο, δ ^ / ο and having a temperature of about 300 ° C.

The blast gas initially formed in the first fuel bed, which is burned by the upper wind, contains on average 11% C 0 + H ₂ . At the end of the blistering period, this content rises to around 30%. The ratio of the amount of wind above to below wind is 0.9: 1 at the end of the blowing period, while it is 0.25: 1 over the average for the entire period.

During the blowing process, an amount of heat of around 830,000 kcal is stored in the first fuel bed. From the sensible and combustion heat of the primarily formed blown gas more fall 2175,000 kcal, of which 1322,000 kcal in the heat storage and 545,000 kcal collected in the second fuel bed, while 308,000 kcal as tactile Heat can be discharged with the blowing gas. Around 2,340,000 kcal are available for water gas formation Disposal.

In a complete gasification period 1.435 t of coke of the grain class 20 to 80 mm and gasified with a carbon content of 85%. 33% of the carbon is distributed to the blown gas and 67% on the water gas.

The heat balance of a gasification period is as follows:

Heat brought in:

Calorific value of 1,435 kg of coke 9,890,000 kcal

Sensible heat in the gas vapor

(150 ° C) 108,000 kcal

Total heat input .... 9,998,000 kcal

Dissipated heat:

Calorific value of the water gas (H ₁₁ ) 8150000 kcal - 81.50%

Calorific value of the blowing gas

(0.8% CO) 71000kcal - 0.71%

Tangible warmth of the
Water gas 615,000 kcal - 6.16%

Tangible warmth of the

Blowing gas 308,000 kcal - 3.08%

Wall losses of the gas generator 554 000 kcal - 5.55%

Unburned in the

Slag 300,000 kcal - 3.00%

Total applied 9,998,000 kcal - 100.00 per cent

With the same shaft dimensions and roughly the same Water gas output per hour, the gas generator operated according to the invention gives a gasification efficiency of 81.5% compared to only at best 65% with the previously known systems. The investment costs are also lower, since only one instead of two to four heat accumulators or ignition chambers is available. In addition, the relatively expensive waste heat boilers are omitted, since the lower ones do Outlet temperatures of water gas and blown gas no longer worth using the waste heat, except for drying or similar purposes where high temperatures are not important.

The gas vapor must therefore be made elsewhere than the one in the water jackets The amount of steam produced by the gas generator is at best 2 to 3 t / h, while 8 t of gas steam per hour are needed. Taking into account the possibility of the water vapor in an existing To produce a boiler house from cheap fuel, the increase in the gasification efficiency results in a cheaper water gas to around 85% of the previous generation costs.

It also helps to further reduce operating costs if, as in the previous variously indicated, the expensive fuels, such as coke, anthracite, etc., replaced by others.

The following options can be considered for this:

1. Lumpy raw coals of all kinds, including ίο lignite and high-bituminous, heavily baked coals Hard coals.

In the case of lignite and other highly reactive fuels, the increased conversion of CO ₂ to CO during blowing is taken into account by correspondingly increased headwinds, as is the case with lower blowing speeds.

The formation of load-bearing ceilings and agglomerations in the fuel bed when using bituminous coal is prevented by one

ao either gives up a certain amount of Alenge coke at the same time as a lean agent or inactive, incombustible Substances in coarse-grained form, such as slag, chunks of fireclay, gravel or even metal ores, which can be roasted in this way and later separated from the slag. The slag will then discharged from each fuel bed at their lowest temperature, namely at the end of the gassing.

While when only coke is used, the task is done at the start of blowing of uncoked fuels expediently towards the end of the blowing process. It then happens before the gassing already a certain preheating of the same without a significant part of their degassing products in the gas blows over. Depending on whether the hydrocarbon-like degassing products of the fuel to be preserved as much as possible or to be converted into hydrogen and CO, · the fuel is fed into the second or first gas generator. In the latter case they go Hydrocarbon vapors with through the heat storage and experience a strong breakdown. For example is this necessary for the production of synthesis gas for nitrogen plants, whereby the Methane must be destroyed to below 1% in the gas. Otherwise, if it is as hot as possible When water gas arrives, as for gas utilities, the hydrocarbon vapors are released of the fuel in the second gas generator is only passed through its fuel bed and largely spared.

2. Fine-grained to powdery solid fuels of the type mentioned, including coke breeze are expediently largely abandoned in the second shaft during the gassing process, to prevent excessive dust build-up on the heat storage tank. Is also, as already mentioned, during If fine-grained fuel is also used for blowing, its task is in the first shaft indispensable, and precautions must be taken on the heat accumulator to prevent the Remove ash dust from time to time.

3. If substantial amounts or even mostly liquid fuels such as heating oil, tar or other cheap residues or, for special purposes, gas oil or other hydrocarbons are to be gasified, a sufficient height of the fuel bed must be guaranteed despite small amounts of solid fuel, and in turn, it is recommended that the simultaneous addition of coarse-grained refractory material, as mentioned in 1.

909 528/193

Claims (1)

4. The same applies to the use of gaseous fuels such as natural gas, refinery exhaust gases, and coke oven gas etc. The fuels can be given up when gassing in the second gas generator, if one, as already said for 1, wants to conserve its hydrocarbons. You can do the same in the first slot get to the task. In this case you can see the latticework of the heat accumulator on the surface or consistently build from substances that decompose hydrocarbons in the desired direction and catalytically affect completeness. For example, one can improve methane splitting Prepare the inside of the heat accumulator with nickel oxide on the surface. There are also catalysts which promote the formation of certain hydrocarbons, such as ethylene. The catalytically active substances can also have a beneficial effect on the decomposition of water vapor, such as Chromium and iron oxides. This is often expedient because the process described last the formation of water gas preferably takes place in the heat accumulator. By appropriately chosen The length of the gas and bubble period can also adjust the temperature control of the gas generator to the desired level Adjust conditions. 5. Since the temperature of the slag produced is very low and there are no other obstacles, you can go to the gas generator of the type according to the invention also completely inferior fuels, such as middle products from coal washing plants etc. with an ash content of 50% and above can be gasified very economically. the Strong dilution of the carbon in the fuel bed results in a particularly favorable temperature distribution when blowing, and the drop in performance of the gas generator can optionally be caused by the addition of fine-grained or liquid fuel when gassing, as it is not large. It falls in In any case, a gas that is practically free of dust, since this in the second fuel bed, as in one Filter, is retained. Patent claims: 1. Process for the production of water gas in two gasification shafts, which during the in alternating order of the two shafts and gassing taking place in the opposite direction are connected in series via a heat accumulator that connects their upper parts, characterized in that the two gasification shafts also alternate during the Order of the gas chambers and blowing in the opposite direction the heat accumulator are connected in series and that the blast and / or the gas vapor partly below the fuel bed of one shaft, partly above the fuel bed of the one or both shafts can be fed. 2. The method according to claim 1, characterized in that after each one or more complete Gasification periods - consisting of bubbles and gases - the direction of flow of the Gases are changed. 3. The method according to claim 1 or 2, characterized in that after each time hot blowing the direction of flow of the gases in the heat exchanger is reversed by a switching element will. 4. The method according to any one of claims 1 to 3, characterized in that the quantitative ratio of the under the fuel bed to the wind blower supplied above the same and / or Gas vapor remains the same during the blowing or during the gassing. 5. The method according to any one of claims 1 to 3, characterized in that the quantitative ratio of the under the fuel bed to the wind blower supplied above the same and / or Gas vapor is changed during the blowing or during the gassing. 6. The method according to any one of claims 1 to 5, characterized in that under the fuel bed and above the same or different types of wind and / or gas vapor is fed. 7. The method according to any one of claims 1 to 6, characterized in that the normal blowing wind atmospheric air and / or other oxygen-containing gas mixtures can be used. 8. The method according to any one of claims 1 to 7, characterized in that purer than gas vapor Water vapor and / or gas mixtures are used, the water vapor and / or carbon dioxide contain. 9. The method according to any one of claims 1 to 8, characterized in that the blowing wind and / or the gas vapor can be used without being preheated. 10. The method according to any one of claims 1 to 8, characterized in that the blowing wind and / or the gas vapor is preheated to 250 to 900 ° C before use. 11. The method according to any one of claims 1 to 10, characterized in that the fuel the gasification shafts is separated and abandoned from above. 12. The method according to any one of claims 1 to 11, characterized in that in addition to coarse-grained, fuel forming a solid fuel bed fine-grained to powdery solid, liquid and / or gaseous fuel is used. 13. The method according to claim 12, characterized in that the coarse-grained and the fine-grained, liquid and / or gaseous fuel at different times and at different times Places the gas generator is abandoned. 14. The method according to any one of claims 1 to 13, characterized in that in the discharged slag contained, unburned fuel fractions and the gas generator to be abandoned again. 15. The method according to any one of claims 1 to 14, characterized in that the gas generator In addition to fuels, coarse-grained, refractory materials such as slag, fireclay, natural Minerals or the like., Are abandoned. 16. The method according to any one of claims 1 to 15, characterized in that the of the Outer wall of the gas generator and heat accumulator dissipated heat, the sensible heat of the Water gas and / or the blowing gas and the chemically bound heat of the latter for preheating the gasification agent, for steam generation or other thermal engineering purposes. 17. Device for performing the method according to one of claims 1 to 16, characterized characterized in that the occupancy of the heat accumulator wholly or partially from catalytic