DE2634670A1 - Simultaneous gasification of liquid and solid feeds - in a fluidised bed gasifier - Google Patents

Abstract

Prodn. of synthesis gas comprises continuous simultaneous gasification of liq. and solid carbonaceous materials with an O2-contg. gas and steam in a gasifier-contg. a fluidised bed of the solid material surmounted by a gas phase at a max. temp. of 816-1316 degrees C. The liq. material is injected into the gas phase in the vicinity of the upper boundary of the fluidised bed in such a way that a substantial proportion of the liq. material contacts the upper boundary in liq. form. Depending on the gasification conditions, the prod. gas can be used as a fuel (e.g. with a heating value of >2670 kcal/Nm3) or for methanol or ammonia synthesis. Rapid mixing and temp. equilibration occurs at the gas/dense phase interface, giving high gas prodn. rates from both the liq. and the solid feeds.

Description

Process for the simultaneous gasification of liquid and solid

carbonaceous material The invention relates to a method for continuous simultaneous gasification of liquid and solid carbonaceous Material through selective introduction of the liquid carbonaceous material into a fluidized bed of the solid carbonaceous material to form a carbon monoxide, hydrogen and, if desired, ethane-rich gas.

The fluidized bed used in the process of the invention is used with advantage for the gasification of finely divided, carbonaceous material. It includes a lower, dense fluidized bed of the material and an upper, dilute gas zone with discharged fine grain, which is adjacent to the upper phase boundary of the bed.

The fluidized bed shows a clear upper phase boundary or surface, which looks like the surface of a strong boiling liquid. In general, the height of the fluidized bed is about 1.3 or 1.5 to 3 times as high like the bed in compact form. The bed losses are not only caused by that solid material, e.g. B. coal, is converted to product gas, but also by the Deduction of ash particles (if there is ash in the coal) from the lower part of the bed and by removing smaller particles associated with those in the carburetor upward flowing gases are discharged. The bed is therefore equipped with additional, finely divided, carbonaceous material, e.g. B. Coal, replenished so product gas generation is maintained.

An object of the present invention is to provide an effective one Process for the continuous simultaneous gasification of liquid and solid, carbonaceous material under selective conditions and implementation of essential Amounts of both materials to synthesis gas, i.e. one to carbon monoxide, hydrogen and possibly methane-rich gas. Another task is to create a procedure using a fluidized bed for the intimate mixing of the finely divided, solid and liquid, carbonaceous material, creating a uniform Temperature of the liquid, solids and gases is favored and the gasification conditions can reach equilibrium in a short time.

Another task is to create a method with increased Gas generation per unit cross-sectional area of the reactor and with a reduced Total compression effort in the gasification plant. Another task concerns the creation a process that involves the production of a gas mitb! U calorific value, e.g. B. more than 2,670 Kcal / Nm3 is allowed. Another job is the creation of a process in which numerous varieties and a wide range of grain sizes of the solid, carbonaceous material from lignite to coal and coke, baking and non-baking coals and coals with a high ash content, as well as very diverse ones liquid, carbonaceous materials can be gasified. Another job consists in the process in a single-stage fluidized bed of finely divided, carbonaceous Carry out material and thereby a high product gas generation per reactor cross-sectional unit to achieve the system size required for a given gas volume reduce to a minimum.

Another object is to create a method at that of the surface of the fluidized bed formed from the solid, carbonaceous particles as a reaction surface for the reaction between the liquid, carbonaceous Material and the oxygen-containing gas used in the fluidized bed is used, so that in this way simultaneously with the synthesis gas production from the carbonaceous Solid particles also make synthesis gas from the liquid material.

Another object is to create a process for continuous Introduction of fine, solid, carbonaceous material into one Fluidized bed, resulting in continuous, efficient fluidized bed operation, a uniform temperature between solids and gases is favored and the gasification conditions can reach equilibrium in a short time. One another task concerns one Process in which volatile constituents containing, solid, carbonaceous material without its pretreatment for the purpose Removal of the volatiles used before introduction into the fluidized bed can be. Furthermore, baking coals should also be able to be used, with the tendency of these coals to agglomerate and form large ones that are difficult to whirl up Pieces must be reduced.

Another object of the present invention is to provide one Method using a pneumatic delivery system, wherein the fluidized bed operation carried out under pressure and the printing system can be completely closed. In contrast to screw conveyors, the external motors and the like and therefore The pneumatic supply of pressure seals is also required for seals relatively free. The pneumatic feed can also be used with a lock bunker system Apply to coal from ambient pressure to the increased pressure of the fluidized bed bring to.

Another task is to create a process that works together Multiple stages (strands) can be operated, as is the case with the present large capacity required for technical operating systems with acceptable economic efficiency to reach. Another task is to create a process that in manufacturing processes, in particular for the technical production of heating gases with low / medium calorific value, methanol or ammonia economically integrated can be made so that these products are inexpensive be generated. Another object is to provide a method of making Heating gas with a high conversion of the fuel fractions (e.g. 85 to 90%) into a heating gas with a high calorific value can be achieved.

According to the process according to the invention for continuous, simultaneous Gasification of solid and liquid, finely divided, carbonaceous material under selective conditions to form one rich in carbon monoxide and hydrogen Product gases are these materials, steam (the underlying fluidizing medium) and the oxygen-containing gas (the underlying gasification medium), with controlled Feed speeds and under certain conveying conditions in a closed Carburettor introduced. The carburetor has a limited fluidized bed of the material as a lower, dense phase with an upper and a lower phase boundary. Gases, which escape from the fluidized bed and take particles with it, form in the gasifier essentially containing an upper, thinned, discharged, finely divided material Gas zone which adjoins the upper phase boundary of the fluidized bed.

The liquid, carbonaceous material is close to the upper phase boundary of the fluidized bed and introduced into the gasifier with the direction of this phase boundary, preferably in the form of fine spray droplets, e.g. B. Droplets in a range of sizes from about 10-500 microns. The liquid material is moving at sufficient speed introduced so that it comes into contact with the surface of the particles in the bed and this surface can serve as a reaction site. The introduction takes place in a such Amount that increases the amount of gas generated in the carburetor will.

The liquid carbonaceous material generally has a Temperature in the range from ambient to about 4270C, preferably in the range from about 93 to 3160C. It is preferably as high as possible Temperature preheated to favor the beginning of its conversion in the carburetor, however, temperatures should be avoided at which during conduction (movement) of the material in the injection system leading to the carburetor thermal cracking occurs so that you get maximum thermal efficiency of the entire system. The material is preferably transported at a speed sprayed onto the bed, generally in the range of about 6.10 to 30.5 m / s, preferably in the range of about 12.2 to 18.3 mis. The injection takes place in an amount sufficient to increase gas production, which is included in the generally in the range from about 0.01 to 20, preferably from about 0.1 to 1 kg, per kg of the solid, finely divided, carbonaceous material fed to the bed lies.

The liquid, carbonaceous material increases as a reactant the proportion of methane and carbon monoxide among the carbon compounds of the product gas. The calorific value of the product gas can be 1.5 times the calorific value of a gas from a exceed the same gasification process without the use of liquid hydrocarbons. The liquid, carbonaceous material leads to elevated temperatures, in particular right away above its lead-in zone. Therefore do not succumb converted carbon valuable substances passing through the zone of elevated temperature stricter reaction conditions, so that the conversion of the carbons is favored will. The method according to the invention increases the product gas generation per unit volume of the reactor, and there will be a better conversion of the fuel recyclables to one Product gas with a higher calorific value than with conventional vortex processes is achieved.

The liquid, carbonaceous material can be stored at room temperature, i.e. at 250C, normally liquid hydrocarbon containing material be. It can be a hydrocarbon, e.g. naphtha, kerosene, coal tar, heavy oil, Heating oil or gas oil, residual oil or the like. It can be predominantly aromatic or be aliphatic and contain bound oxygen, such as. B. alcohols etc. The carbon-containing liquid can also be the volatile component, for example be made from coal obtained by thermal pretreatment of the raw material, before it was used in the gas generator.

The volatile components can also come from other carburetors, where they were released and collected. The liquid, Carbonaceous materials are heated to give them a sprayable texture admit; Steam can also be used to atomize the carbonaceous liquids can be used. The amount of liquid hydrocarbon depends on the desired Results.

It can be about 1 to 95%, preferably about 10 to 50% of that of the carburetor added carbon recyclables. The amount of the liquid hydrocarbon shouldn't be so big that Hydrocarbons from the carburetor emerge, as they are then arranged in processing systems arranged on the downstream side of the gasifier can condense.

The solid, finely divided, carbonaceous material, e.g. B.

Coal, pneumatically introduced into a fluidized bed using a pneumatic supply system under selective conditions that allow heat transfer from the fluidized bed on the coals located in the feed system, while at the same time substantial amounts of coal introduced into the fluidized bed volume, with the Bed can be quickly mixed and absorbed by this.

A carrier gas is advantageously used together with the coal in the system applied. The fluidized bed operation takes place in a gasifier tank. The heat transfer from the gasifier to the coal / gas medium in the feed system is inhibited as he could lead to coal agglomeration.

The selective conditions include a correlation between the pressure drop (PD) per effective unit length of the line, that in the carburetor applied pressure, the ratio of coal to carrier gas and the carrier gas temperature for a given particle size range of the coal used.

The pressure drop in the system i.e. the pressure drop between pressures at the point of loading the solid material into the carrier gas and the pressure in the carburetor is such that it does not exceed the absolute pressure in the carburetor; he is usually in the range up to about 5, e.g., 0.1 to 5 atmospheres each according to carburetor pressure. The higher the pressure in the carburetor, around the greater the pressure loss that occurs. The pressure loss is sufficient, the coal / gas medium to be introduced into the fluidized bed a good distance away from the gasifier walls and the transfer of radiant heat from the bed to the supply line increases significantly inhibit. The pressure drop is determined by the location or

the points downstream of the entry point (s) into the carburetor regulated on the or on those in the pneumatic supply line in the carburetor coal to be introduced is mixed with or introduced into the carrier gas.

The carbon-containing carrier gas is below and / or above the upper Phase boundary of the fluidized bed introduced directly into the gasifier. It is under overpressure introduced, generally at a pressure somewhat above that prevailing in the carburetor Pressure, e.g. B. generally between about 1.05 and 105 at, depending on the operating pressure. The finely divided coal is in the line in the carrier gas in the ratio of about 3.2 to 32, preferably from about 4.8 to 24 kg coal per m3 of carrier gas, i.e. per m3 Carrier gas under the prevailing conditions, suspended. The carrier gas can expediently be heated to preheat the finely divided material, for example to temperatures from about ambient to about 2040C or 3160C or about 5380C.

The fine material carried away with the carrier gas is essentially continuous velocity introduced into the fluidized bed and so into the gasifier maintain stationary operation. The finely divided material is in sufficient Quantities supplied so that the upper phase boundary remains at a given level, for example about 1.22 to 6.10 m above the lower phase boundary of the fluidized bed, the height ratio of the diluted gas zone to the fluidized bed ranges from about 3: 1 to 10: 1. The fine material becomes sufficiently wide introduced into the carburetor away from the carburetor walls, i.e. blown or thrown in, so that an impermissible agglomeration on the carburetor walls, in particular near the insertion point. Containing volatile components finely divided material can become sticky when heated to gasifier temperatures; if such sticky particles touch the walls of the carburetor, they can stick to the Walls stick and agglomerated approaches can grow. Therefore the finely divided material is preferably introduced in such a way that it enters the fluidized bed arrives without at the site of insertion or diametrically opposite to a significant extent to hit the carburetor walls as long as not all of them are essentially volatile Components are released from the material. This is done appropriately finely divided material directed downwards, e.g. B. in a horizontal and downward direction Direction, one to get the desired quick mixing with and inclusion of the To favor the mass of the bed and the possible, impermissible growth of agglomerated Avoid material at the insertion site. For example, if the injection nozzle is directed downwards, the action of gravity aids in the removal of the Material from the vicinity of the feed point.

The finely divided, carbonaceous material, e.g. B. Coal, has im generally a particle size in the range of 0 to about 9.5 mm and is expediently fed into the gasifier pneumatically by inputting it into the carrier gas flow introduced, preferably in a heated gas stream, which is used to preheat the coal serves.

Suitable carrier gases are inert gases, carbon dioxide, recycle gases and preferably steam or mixtures of steam and air, oxygen or oxygen enriched air, depending on the reactivity of that introduced into the fluidized bed Money.

For example, if the coal is relatively inactive, a It is desirable to add air or air enriched with oxygen to the carrier gas be to be a non-reactive zone in the bed near the inlet of the gasifier to avoid.

The inventive method is advantageous in a method for continuous gasification of solid, finely divided, carbonaceous material integrated, in which under selective conditions one of carbon monoxide and hydrogen and, optionally, methane-rich gas product is produced. The material, the fluidizing medium and the oxygen-containing gas (the gasification medium) are fed at controlled feed rates and introduced into a closed carburetor under certain feed conditions. The gasifier contains a limited fluidized bed of the material as the lower density Phase with an upper and a lower phase boundary. Those from the escaping Discharged particles entrained gases form in the carburetor essentially one upper, dilute, discharged fine-particle material containing gas zone, which at the upper phase boundary of the fluidized bed is adjacent.

The solid, carbonaceous material is blown into below the bed with selective amounts of fluidizing medium and oxygen-containing gas selective conditions degassed, carbonized, oxidized, hydrogenated and gasified, and the liquid, carbonaceous material is volatilized, cracked, oxidized and reformed (these processes are summarized below under "gassed"). The crude product gas is generated under selective conditions to prevent undesirable formation to exclude heavier hydrocarbons as by-products.

The gaseous crude reaction product flows through the dilute gas zone, so that the top product is a gaseous, carbon monoxide and hydrogen and if desired Methane-rich product, which is usually undesirable finely divided material (e.g. partially consumed coal), and the bottom product is an ash product (e.g. partially used coal), which consists of particles larger than which are in the fluidized bed. The ash product travels down and through the bed is discharged at the bottom of the carburetor. The top product leaves the carburetor below Operating pressure and high temperatures (e.g. approx. 815 to 13160C). The product gas is cooled (to temperatures of around 93 to 260 ° C), whereby its heat content is recovered and removing significant amounts of partially used coal. The won Heat is used to advantage to generate steam, part of which is in the Process is consumed. The cooled product gas that is in a heat recovery zone has been cooled and is under the pressure of the heat recovery zone which is less than the pressure in the carburetor is benefited by a heavy duty washer piped with high pressure loss, to fine, partially consumed Remove coal particles and recover a product gas that is less than about 3.53 (e.g.

less than about 0.35) solid particles per Nm3 gas, at least about Contains 10 vol .-% carbon monoxide and at least about 10 vol .-% hydrogen and one Has calorific value of at least about 800 Kcal / Nm3. The pressure in the carburetor will be with advantage maintained by a back pressure control applied to the gas system takes place at one point downstream of the carburetor.

The solid carbonaceous material can be coke or coal or others solid materials consisting essentially of carbon. The coal can be baking, moderately baking, and non-baking. If baking charcoal is used, care must be taken to ensure that the feed material that is introduced into the carburetor is exposed to elevated temperatures, does not experience harmful agglomeration. Typical Coals are lignite, sub-bituminous and bituminous coal, etc. In general the more reactive, the lower the gasification temperature required the coal is. The carbonaceous material may contain ash, as after present procedure the ash is removed from the gasifier, albeit with the ashes also experience a loss of sensible heat.

The carbonaceous material fed to the carburetor can vary Quality, and the process can be easily operated without physical change switch from one type of coal to the other. To simplify the discussion, treated below as an example of carbonaceous material coal.

The fluidized bed used according to the method can be very different Process coal particle sizes; there can be fine and coarse particles at the same time can be used. The coal fed to the gasifier is generally in that Diameter size range up to 9.5mm. Often the mean particle size is about 2.4 to 4.8 mm. The coal can be dry, e.g. a moisture content of have less than 10 wt .-%, although not before the supply to the gasifier drying is always necessary. The feed charcoal can often be up to 25 or Contain 30% by weight or more of water.

The fluidizing medium is basically steam, which also acts as a reactant serves. It can also be air, carbon dioxide or recycle gas, each with or without steam be. For the sake of simplicity, the vortex medium is hereinafter exemplified as Steam specified. Steam is particularly suitable as a fluidizing medium; it can also be called Diluent gas are used for the gasification medium as it condenses and from the product gas can be easily separated, leaving behind a product gas with a higher calorific value.

Steam is and can be readily available even with the pressures applied with the help of the waste heat generated by the total exothermic Nature of the procedure arises.

The gasification medium is in principle the oxygen-containing gas; it also contributes to the bed swirling. It contains free or bound Oxygen available to react with carbon. It can be oxygen be or oxygen with diluents, for example air or with oxygen enriched air. Preferably it will be on several spatially separated Bodies introduced into the bed. Can diluents for the gasification medium are used, and in amounts that are greater than those for the gasification reaction required amount. Carbon dioxide, recycled product gas, nitrogen and the like can be used. Steam is preferred, however. Inactive diluents, like nitrogen, reduce the temperature in the gasifier and set the calorific value of the product gas per gas volume unit. A diluent, such as carbon dioxide, can take part in the reaction with the formation of carbon monoxide; such Reaction is endothermic. When the product gas can be brought to line quality should, e.g. should be a heating gas with a medium calorific value (about 2490 Kcal / Nm3) an oxygen-containing gas that contains as much nitrogen as air is not permitted. On the other hand, if the product gas is used for synthesis purposes, e.g. for ammonia is to be, air enriched with oxygen can be suitable as an oxygen-containing gas however, oxygen is preferred. If the desired product is methanol, it is preferred to use oxygen alone. Air is suitable for manufacture from heating gas with a low calorific value or from fuel gas (approx. 1110 Kcal / Nm3). if the oxygen-containing gas contains diluents, must for the desired Pressure in the carburetor a larger volume of gas can be compressed.

When air is used as the oxygen-containing gas, it is preferred Air together with steam as a fluidizing medium; if oxygen as containing oxygen Gas is used, steam is preferably used alone as the fluidizing medium.

The primary gasification (e.g. oxidation or reaction) of the coal he follows in the fluidized bed. The coal particles gasified in the bed have a mean one there Residence time of about 30 to 100 minutes. This residence time is much longer than the residence time of the gas product (about 2 to 50 seconds). The residence time given Particle in the bed is sufficient to make up substantial amounts of the available carbon to oxidize to carbon monoxide. The bed experiences a strong emotion, the primary one takes place through the fluidizing medium with the aid of the gasification medium.

As mentioned above, this agitation can be described as a boiling motion will.

The oxygen-containing gas, preferably up to about 50% by volume Steam, and generally with an average overall temperature of up to about 5380C, preferably from about 38 to 5380C and at a pressure slightly above the carburetor pressure, is preferably at spatially separated evenly distributed over the circumference Places introduced into the carburetor at different heights, and in quantities that sufficient to make it selective with the components of the fluidized bed under controlled Bring reaction conditions evenly into contact and these components to gas. The temperature of the oxygen-containing gas should be achieved a maximum overall efficiency in this area must be as high as possible. Preferably at least about 50% by weight of the steam supplied to the fluidized bed is used at the lower phase boundary of the fluidized bed at spatially separated, essentially places evenly distributed over the circumference, generally at one temperature up to about 6490C and a pressure slightly above the carburetor pressure and speed introduced to the It is sufficient to swirl the lower part of the bed.

Every place of the bed is due to the created by the fluidized bed Stirring strives to assume the same temperature with respect to the time. However, you can the composition of the vortex medium and the distribution points for the introduction of the fluidizing medium in the bed serve to change the temperature profile in to reach the bed, which can lead to product gases of different quality. For example, the coal particles in the lower part of the bed can be steamed get in touch. The steam is preferably blown into the lower level of the bed, to stir up the particles and preferably heat from those at the bottom of the bed extracting ash particles (e.g. particles from partially used coal) and to cool these particles and thus preheat the steam. Similarly, can a portion of the oxygen-containing gas is fed to the upper part of the bed, to oxidize the remaining carbon. Further proportions of the oxygen-containing Gas with up to about 10 volume percent steam, e.g.

with about 0.1 to 10 vol .-% steam, can at or just above the Phase boundary between the fluidized bed and the dilute phase at spatially separated, substantially evenly distributed over the circumference in sufficient places Quantities are introduced so that they are with the carbon fractions leaving the fluidized bed react, increase the temperature in the dilute phase, the carbon turnover of the process and provide a crude product gas that is at least about 50% of the oxidized carbon as carbon monoxide.

The area of the bed adjacent to the phase interface, i.e. the interface between the bed and the dilute-phase gas zone can generally be higher Have temperatures, since this is where the primary oxidations take place and this area is in contact with the hot reaction gases from the lower parts of the bed.

The gasification reactions occurring in this process include the oxidation of carbon as well as the reduction of carbon dioxide to form a Product gas, which essentially contains carbon monoxide and hydrogen. The starting materials are coal, liquid, carbonaceous material and oxygen that is released by the Oxygen-containing gas and steam is supplied. The basic gasification reactions are as follows: C + 02 = C02 (exothermic) C + 0.5 02 = CO (exothermic) C + C02 = 2 CO (endothermic) C + H20 = CO + H2 (endothermic) C + 2 H20 = C02 + 2 H2 (endothermic) C + 2 H2 = CH4 (exothermic) The rates of these reactions are increased by Temperatures favored. The coal in the fluidized bed is with advantage in one Maximum temperature in the carburetor in the range of about 816 to 13160C gasified. The main temperature in the dense phase is preferably below the softening temperature the ash arising from the solid or liquid material. It becomes a gaseous one Reaction product produces which is carbon monoxide, hydrogen, carbon dioxide, methane and Contains diluent and passes into the diluted phase.

At the same time, solids arise from gasification from partially used solids Money. The temperature in the dense phase of the gasifier is preferably about Maintained 28 0C below the softening temperature of the ash. The temperature used depends on the amount of diluent gas in the fluidizing and gasifying media, the Type of coal, the softening temperature of the ash, the heat tolerance of the gasifier and the like. Generally, the temperature will be at least about 816 up to about 13160C or more, and to achieve good thermal performance, preferably about 927 to 1093 or 1204 ° C. The diluted phase advantageously has the highest possible Temperature as far as this is compatible with the properties of the ash it contains.

Temperatures are to be avoided, depending on the one used carbonaceous material to condensable hydrocarbons in the product gas lead and on the other hand are too high and a reduction in the overall efficiency of the procedure. If methane production is intended, be temperatures in the range of 815 to 9270C are preferably used.

The liquid hydrocarbon is close to the phase boundary between the dense and the dilute phase distributed. Due to the high temperatures of the carbonaceous material and the gases in the distribution zone becomes the liquid Hydrocarbon volatilizes quickly and enters the gasification process. Since the distribution zone of the liquid hydrocarbon is generally a low one Concentration on free Has oxygen, one combines significant amount of the hydrocarbon with carbon dioxide to form carbon monoxide and water. The presence of free oxygen supports the exothermic oxidation of the Hydrocarbon to carbon monoxide, water and hydrogen.

The reactions in the carburetor are advantageously under excess pressure generally above 1.5, for example from about 1.5 or 2 to 20, with Advantageously from about 2 or 2.5 to 15 and preferably from about 6 to 14 ata. The selection the pressure applied in a given system depends on the design and the pressure tolerance in the processing plant, the pressure drop in the plant on the downstream side the gasifier, the desired special use of the product gas and the like. as well as whether multiple carburetors are used in strings.

The use of higher reaction pressures according to the invention favors also the degree of utilization of the coal for product gas generation and increases the gasifier throughput.

In this process, selective amounts of coal, liquid, carbonaceous Material, oxygen-containing gas and steam as a function of several variables used to determine the operating conditions (e.g. temperatures), the calorific value of the product gas and maintain production speed. The total amount of steam used should be sufficient to keep the bed in the desired vortex state and condition Keep temperature. There is a particular advantage of the present method in that the steam required for the fluidization and gasification through utilization the Process heat for steam generation can be obtained. Here falls a cooled product gas, preferably having less than about 141 particulate matter per Nm3, for example for gasification pressure and for those that are better suited for further processing Temperatures, with substantial amounts of partially consumed coal from the Crude product gas for the purpose of removal from the process, recycling or work-up removed under other conditions and the cooling of the product gas to temperatures from about 93 to 260C in a heat recovery zone. There can be an excess of high pressure steam can be generated in excess of the amount required in the process. This excess is therefore used to drive the turbine for product gas compression and available in the case of using air to drive the air compressor. Generally, up to about 60% by weight of partially spent coal becomes from the ground of the bed withdrawn and advantageously with at the lower phase boundary in the bed brought into contact with introduced steam, creating the sensible heat of the consumed Coal is extracted and used for steam preheating.

The ratio between coal and oxygen-containing gas should be the generation of a sufficient amount of heat through oxidation reactions for the Allow maintenance of gasification; however, the amount of heat should be less than be the amount of heat that would lead to excess production of carbon dioxide (e.g., less than about 15 to 20 volume percent). At a constant coal feed rate is used to maintain the ratio of oxygen-containing gas and steam to coal the desired bed temperature is selectively regulated.

If air is used as the gasification medium, it can be used for the provision the air required for coal gasification is advantageously used with compressors find that are powered by a steam turbine. As mentioned above, you can additional proportions of steam or oxygen-containing gas also on or in the vicinity the bed surface are selectively injected in order to be discharged into the dilute phase To further gasify carbon particles. This injection is sufficient Height, so that a further gasification of the carried coal particles and a separation part of the solid material carried away is possible.

The gas and particles carried out from the fluidized bed form immediately above the bed, a dilute gas zone containing discharged particles. In contrast to the bed, this dilute phase has no upper phase boundary or Surface. Rather, it expands into the closed gas generator given space; its dimension is therefore determined by the dimensions of the surrounding Carburetor determined. The entrained particles are usually taken along with the Product gas withdrawn from the dilute phase.

The level of the diluted phase containing the entrained particles ensures that the particles have an additional period of time under the gasification conditions remain so that the gasification continues and part of the solid material from the dilute phase returns to the bed before the product gas enters the gasifier leaves. The amount of the diluted phase compared to the bed can be varied. For example, it can be reduced be to the amount of carried out to increase finely divided material. However, if the level of the diluted phase is insufficient too large amounts of carbon can be lost from the gas generator. That The upper part of the gas generator can have a larger diameter than the lower part, so that the gas velocity decreases and consequently the residence time of the particles increased in the dilute phase and the return of entrained particles to the fluidized bed is favored. With a normal particle size distribution of the feed material about 40 to 70% of the solid material leaving the carburetor in the form of the the diluted phase withdrawn product removed.

In general, the height of the dilute phase is about 3 to 10 times, preferably about 4 to 8 times the height of the fluidized bed. Another Possibility to extend the time in which the fine coal particles undergo gasification conditions are exposed, is the recirculation of part of the separated in a hot cyclone Money.

That from the conversion of carbon, steam and oxygen containing The crude, gaseous reaction product formed in the gas generally has a residence time from about 2 to 50 seconds, preferably about 5 to 30 seconds, in the upper diluted Phase of the carburetor. The superficial velocity of the raw product gas in the gasifier is well above the point of incipient turbulence and is generally sufficient up to about 6 m / s depending on the operating pressure.

The product gas is rich in carbon monoxide and hydrogen and contains generally for example about 50 to 90%, preferably approximately 55 to 85% carbon monoxide based on the total oxidized carbon. Of the The remainder of the oxidized carbon is essentially carbon dioxide. It can too smaller amounts of methane may be present; generally less than about 10% or even less than 6% of the carbon in the product gas is present as methane. Bigger ones Quantities of methane (e.g., greater than about 10% and up to about 35%) can affect methane formation favorable conditions are generated in the carburetor. The presence of the methane is advantageous if the product gas is used as heating or fuel gas. the The amount of methane produced is determined by the operating conditions used in the gasification influenced.

Favorable conditions for methane formation are the use less Amount of steam (if steam is used), whereby the amount of steam omitted is entirely or partially replaced by recycle gas, temperatures in the range of about 816 to 9270C and pressures in the carburetor of at least about 10 ata. Furthermore, preferably part of the coal above the upper phase boundary of the fluidized bed introduced.

In the production of heating gas according to the method according to the invention desulfurized the cooled product gas if desired.

A two-stage desulfurization process is expedient applied, the first stage being the sulfur compound in the form of an acidic gas, namely supplies as hydrogen sulfide, which is then selectively absorbed from the gas will. Carbon oxysulphide can for example by hydrolysis to hydrogen sulphide implemented. The hydrolysis can preferably be carried out in the presence of a carbon oxysulfide hydrolyzing catalyst under a pressure greater than about 4.2 ata at hydrolysis temperature, e.g. around 93 to 2050C. The amount sufficient for hydrolysis Water is often included in the cooled product gas. The reaction is exothermic.

The outflowing product is generally at the absorption temperatures cooled, i.e. to temperatures at which the equilibrium for hydrogen sulfide absorption is cheap.

The gases are mostly at a temperature of around 21 to 380C cooled before they enter the absorption unit.

The absorption can be carried out with a common selective absorbent for hydrogen sulfide. Typical absorption systems are, for example Alkazid Process and the Stretford Process. The absorption is mostly at a temperature of about 21 to 380C, preferably under a pressure of more than 4.2 ata performed. The used absorption solution can be regenerated, whereby a rich gas containing hydrogen sulfide is produced. From the hydrogen sulfide containing gas can be in the usual way, for example by the Claus process, more elementary Sulfur can be obtained; the Claus process can be supplemented by a sulfur dioxide absorption system, so that an exhaust gas that is tolerable for the environment is produced.

The gas from the gasification process can be used to synthesize chemicals such as ammonia and methanol. The general reactions for the production of methanol and ammonia are The cooled product gas is rich in carbon monoxide and hydrogen. Since each of these syntheses requires considerable amounts of hydrogen, the product yield can be improved by converting the gases over a suitable, sulfur-resistant catalyst. During the conversion, carbon monoxide and water vapor react in a molar ratio of 1: 1 to form hydrogen and carbon dioxide. A gas with about 2 to 2.5 moles of hydrogen per mole of carbon monoxide and carbon dioxide is often used for the synthesis of methanol. The shift reaction is often relatively effective, and a product gas stream can be bypassed around the shift reactor and combined with the exhaust gas from the shift reactor, so that a gas with the desired proportions of hydrogen to carbon oxides is produced. No carbon monoxide is required in ammonia production. Therefore, the shift reactor delivers an exhaust gas with less than about 3, preferably less than about 2% by volume of carbon monoxide. The shift reaction is generally carried out at a temperature of about 260 to 4820 ° C. under a pressure of more than 14 ata. It can be seen that increased production of carbon monoxide and hydrogen according to the present invention increases the yield of the synthesis product.

The invention is illustrated with reference to FIG. the drawing and to the Examples explained in more detail. 1 shows a schematic flow diagram of an embodiment of the method according to the invention for the simultaneous gasification of coal and liquid, carbonaceous material under selective Conditions to one product gas rich in carbon monoxide and hydrogen; Fig. 2 is a schematic flow diagram an embodiment of the method according to the invention for producing heating gas and FIG. 3 shows a cross section of the gasifier wall with a distribution nozzle for liquid Hydrocarbon in a schematic representation.

In Fig. 1 is a gasifier 10 with a fluidized bed 12 and a diluted one Phase 14 shown. The lower part of the carburetor is usually frusto-spherical formed, wherein the main part of the bed is located in this conical part. A spray distribution device 15 with substantially uniform over the circumference distributed spray nozzles is on the outside of the carburetor about 60 cm above the upper one Phase boundary of the fluidized bed provided. The spray dispensing device 15 is in spray contact with the upper phase boundary of the fluidized bed and sprays liquid, carbonaceous material on the surface of the particles in the bed on.

The solid material is fed to the gasifier 10 in the following manner. Coal of the specified grain size is fed to the conveyor 16 and to the Feed hopper 18 transported.

The conveyor apparatus 16 can be a conveyor belt, bucket conveyor or the like be. A chain conveyor is expediently used, since this is usually does not jam and does not come to a standstill when the container is full.

The bunker 18 delivers crushed coal to two lock bunkers 20 and 22. In practice, especially when operating at pressures greater than 2.5 ata, it may be desirable to have additional parallel or possibly in series Provide lock bunker so that a continuous coal supply to the gasifier is guaranteed. The lock bunkers enable a pressure increase in the area of the coal to a value suitable for introduction into the gas generator. In general, the coal charge is subject to gas backflow to avoid it a pressure that is greater than the pressure in the carburetor.

Other methods can be used to bring coal to normal pressure to bring on increased pressure.

The lock bunkers work in cycles. In the first stage of the cycle if the lower valve of the bunker is closed and the upper valve is open, see that the lock bunker can be charged. When the lock bunker is charging the upper valve is closed and a gas is introduced to increase the pressure. Finally, the batch is emptied through the bottom of the bunker under increased pressure. The batch falls into the holding bunker 24. The introduction of the pressurized gas, e.g. Inert gases, such as nitrogen or carbon dioxide, can be used in the lock bunker for the purpose Accelerated batch handover to be continued during unloading.

The coal is pneumatically conveyed from the holding bunker 24 to the gasifier 10 through the line 26, the pneumatic supply line, transported whose clear Width from the upstream end point 8 to the point where it joins the carburetor 10 essentially is equal to. The one described above, chosen Pressure drop is maintained between these points to keep the coal in the desired location Way to introduce. The coal can be used for better distribution and with a given product introduced in several places to improve the operating characteristics of the process will. The carrier gas for the pneumatic coal transport can be a mixture of Be steam and oxygen-containing gas. The steam can expediently from a Downstream processing stage, e.g. a waste heat system, with one temperature from 204 to 649 0C. The steam can be mixed with oxygen-containing gas , the line 65 leading through line 64 from the oxygen-containing gas is branched off. The steam and the oxygen-containing carrier gas flow through conduit 25, and finely divided coal from the holding bunker 24 is introduced into the carrier gas flow, so that there is a relatively high solids content in the carrier gas stream, e.g. about 3.2 to 32 kg of solids per m3 of carrier gas under the prevailing pressure. Of the Stream containing solids passes through line 26 to gasifier 10. Line 26 placed near the nozzle through which the coal is fed into the gasifier, cooled (not shown) The cooling is sufficient to keep the solid coal particles in to keep the stream entering the carburetor in a free flowing state and heating by the heat prevailing in the gasifier up to the agglomeration point to avoid the solids. When coal containing volatiles is heated, temperatures can generally be reached at which the carbon surface becomes soft and sticky so that the particles can stick together. Larger agglomerates are to be avoided in the fluidized bed as they are not under the prevailing conditions above be whirled up for a sufficiently long time for gasification can. Too much agglomeration can also lead to nozzle clogging. A fluid coolant, e.g., low temperature steam, is supplied through line 27 supplied, flows around the nozzle and is withdrawn from the nozzle through line 29. Alternatively the coolant can be water or another fluid.

The swirl gases are often blown into the carburetor at several points. In this way the reaction of the dense bed phase can be controlled so that the coal utilization increases and a high quality product gas results. As shown, a stream consisting essentially only of steam (100%) is passed through Line 28 introduced at the lower phase boundary of the fluidized bed. The steam serves not only as the primary fluidizing gas, but also for cooling the ash particles (e.g. also particles from only partially used coal) for the purpose of discharge the lower part of the gas generator. Oxygen is supplied through lines 30, 32 and 34 Introduced containing gas, which also contain the steam as a diluent can. The oxygen and the diluent steam aid the gasification and carry along with other diluents in the oxygen.

containing gas for bed fluidization and temperature control. Line 34 carries the oxygen-containing gas preferably at or just above it the phase boundary between the bed 12 and the dilute phase 14 to. The gas inlets are often semi-tangential nozzles. To ensure a good emotion, the Fluidized bed generally has a ratio of height to maximum diameter of about 1: 2 to 5: 1. The dilute phase gas zone contains entrained particles from the bed.

The liquid, carbonaceous material comes out of the storage tank 35 through the line 37 with the valve 39 into the gas generator and is through the Spray distributor 15 distributed. 3 shows the spray distributor connected to the carburetor 17 15 more precisely. The liquid, carbonaceous material is preferably distributed relatively evenly, creating one over the cross section of the gas generator uniform temperature is favored. The flow of the liquid, carbonaceous Material from the manifold is preferably countercurrent to the gas flow. The liquid, carbonaceous material is sprayed onto the bed so that the particles in the bed come into contact with it and become coated with it. Because of the boiling motion of the bed, essentially all of the particles come in the bed comes into contact with the material after a while.

The liquid, carbonaceous material occurs in the form of a fine Spray through the nozzles of the spray manifold 15 in a downward direction. In general the feed is 1.34 10 2 to 6.67 102 l / m3 of gas product. The generated spray generally comprises an arc of about 600 to 1200, e.g., 900, the spray droplets generally range in size from about 10 to 500 microns, the preferably come into contact with the particles in the bed.

As shown in the drawing, the spray dispenser is located 15 sufficiently close to the upper phase boundary of the fluidized bed, and it becomes an uninterrupted one Spray generated from liquid, carbonaceous material at such a rate that the upward velocity of the evolved gases, e.g. about 15.25 m / s, was overcome will. The liquid reaches the upper phase boundary of the fluidized bed, comes with it her in contact and penetrates due to the turbulent mixing effect of the bed in the downward direction into bed. In general it is the velocity of the liquid to the bed so large that a substantial amount, e.g., at least 20%, preferably about 50 to 80% depending on the volatility of the liquid penetrating the bed.

The spray distributor 15 is close to the upper phase boundary of the dense Arranged bed. The upper phase boundary is due to the boiling motion the whirling up in constant motion. The distributor should preferably be within be arranged about 1.53 m from the middle upper phase boundary.

The crude product gas is over after exiting the gasifier 10 Line 36 treated in the cyclone 38. The scheduling of cyclone 38 depends on that used starting material, in particular its grain size, from. The line 40 leads the separated fine-particle material back to the bed, as this material can be recycled May contain carbon. When the separated particulate material in the carburetor is recycled, it is advantageous to maintain the reaction temperature to avoid unnecessary heat loss and carbon expenditure.

The finely divided material separated by the cyclone can be in different Recycled, e.g. as fuel or - in the case of several stages - as a load for another carburetor. The unreacted in the product leaving the carburetor Coal shows a difficult gasability among the Gasification conditions in the carburetor, so it is beneficial to have these materials in a carburetor to be used, which is driven under more severe conditions.

In Fig. 1, the bottom of the carburetor 10 is also provided with a device to remove the ashes. The larger and heavier ash particles are inconsistent and fall out of the fluidized bed. These particles are collected and by a water cooled auger 41 for removal from the system transported to the discharge lock bunker 42.

To reduce the particle size of the ash to an easily transportable one Size a crusher can be provided.

The raw product gas from the gasifier 10 is generated by indirect heat exchange cooled in the heat exchanger 44 with heat recovery. Fine-particle material, which is deposited from the gases during cooling, can be transferred from the heat exchanger 44 Line 46 can be withdrawn. The finely divided material can be handled in the same way become like the ashes at the bottom of the gas generator. The cooled gases leave the Heat exchanger 44 via line 48.

The heat exchange medium for heat exchanger 44 is steam.

Boiler feed water enters the heat exchanger through line 50 44 and, after preheating, it reaches the steam drum 52 via line 54. The Steam drum 52 can be fitted with a radiant boiler (not shown) in the top of the carburetor 20 are in communication. The heat from the radiant boiler can be used for the indirect heat exchange with the steam in the steam drum 52 can be used. Saturated steam generated in the heat exchanger 44 leaves the steam drum 52 via the line 60 and returns to the boiler 44, where he is overheated prior to its delivery to the steam network of the plant through line 62. A Part of the steam from line 62 is mixed with the oxygen-containing gas from line 65 and serves as a diluent when introduced into the carburetor for the gas in lines 30, 32 and 34. Another part of the steam arrives through line 28 to the carburetor. The process can be operated under such conditions ensure that sufficient steam is generated for discharge from the gasifier.

Sufficient sensible heat is available under certain conditions those with advantage for preheating the oxygen-containing gas in the waste heat recovery line or, if desired, can also be used for accompanying procedures.

The cooled gases leaving the heat exchanger 44 pass via line 48 through cyclone 68 and through line 74 to scrubber 72, wherein the cyclone with a line 70 for removing the separated finely divided material (namely partially used coal) is equipped. The bulk of the partial spent coal in the product gas, those in the heat recovery plant and the cyclone was separated, can by a screw conveyor to a coal bunker (not shown) reach. The heat recovery unit and the cyclone can together at least about 50% and greater than 75% by weight of the solids discharged with the product gas split off. In the case of a heating gas system, the coal is transported from the coal bunker to the system boundary, in an ammonia or methanol plant it becomes a coal charging bunker of the coal-fired boiler. A water scrubber is provided to to wash the conveying nitrogen before blowing off.

The scrubber 72 removes particulate matter and condenses steam from the gas. The gas from the cyclone flows through the venturi scrubber 72 where the remaining coal particles to a content of less than 0.035 particles / Nm3 removed. In order to keep the water consumption to a minimum, this is Venturi water is cooled and, after the ash has been removed, it is recirculated in a sedimentation tank. Additional water may be required for the ash container. The coal will in the form of a wet sludge removed from the sedimentation tank and to the system boundary pumped.

High-performance washers can be used. Suitable scrubbers are spray towers, cyclone-like spray towers, venturi scrubbers (e.g. a type with high Effectiveness and high pressure loss) and the like. The venturi scrubber or venturi type Scrubbers are particularly advantageous because they allow for further particle separation from the gases is not required. Electrostatic precipitators and disintegrators were used on the downstream side of the scrubber to remove the entrained Remove particles. The gases leave the scrubber via line 76.

Example I The system shown in Fig. 1 is used for gasifying a Waste oil with about 84% carbon, 12% hydrogen and one upper Calorific value of about 10 000 Kcal / kg together with a semi-bituminous coal with about 50% carbon, 20% ash, 15% water and 10% oxygen and an upper calorific value used dry of 5720 Kcal / kg. The ash has a softening point of 12600C, a melting point of 14270C and a pour point of 14820C. The coal is on broken a particle size in the range of 0 to 9.5 mm.

The carburetor is about 20 m high and has an inside diameter of about 5 m and is conical at the bottom. The top of the fluidized bed is located at a height of about 4 m above the bottom of the gasifier.

About 1,200 t / d coal and 400 t / d waste oil with a temperature of 1490C will. fed to the carburetor (as shown in Fig. 1), which is under a Pressure of about 9 ata is driven. The coal is just below the upper phase boundary of the bed at ambient temperature. The bl is in the form of fine spray droplets sprayed onto the bed with an average droplet size of about 200 microns. To the Gasifiers are supplied with about 11.3 t / h of steam, of which about 5.0 t / h below the Fluidized bed are fed. The coal has an average residence time in the bed of 10 minutes. The gasifier is fed through line 34, 45,600 Nm3 / h of a mixture from about 7% by volume of steam and 93% by volume of air, through line 32, 55,100 Nm3 / h of one Mixture of 7% by volume steam and 93% by volume air and through line 30, 41,900 Nm3 / h a mixture of 3 vol .-% steam and 97 vol .-% air supplied. The steam has one Temperature of about 5380C. The air is through heat exchange with the raw product gas in part of the waste heat recovery system (in Fig. 1 not shown) preheated to 2600C.

The reaction is carried out at 1038 to 11490C. The reaction gases have a residence time in the diluted phase of 15 s; the conduit velocity of the crude product gas in the dilute phase of the gasifier is about 1.53 mis. The gas leaves the carburetor at a pressure of about 9 ata and a temperature from about 9820C. It contains 18 vol .-% CO, 7 vol .-% C02, 11 vol .-% H2, 4 vol .-% methane, 5% by volume N2 and 10% by volume steam.

The waste ash (partially used coal) is collected by the conveyor 41 discharged in an amount of about 3 t / h, it consists of 78 * ash and 22% Carbon. The gas flows through the heat exchanger 44 and the cyclone 68, where heat is obtained from it and further finely divided material is removed. The gas has a temperature of about 1490C when leaving the heat exchanger 44 and contains when leaving the cyclone 68 about 141 dust particles per Nm3. It then gets through the venturi scrubber 72, when leaving the gases a temperature of about 38 0C, a pressure of about 8 at and a dust content of less than 0.035 dust particles each have Nm3. The upper calorific value of the gas is about 1320 Kcal / Nm3. The carbon utilization, calculated from the carbon content of the gas divided by the carbon content of the Oil and coal, is about 93%. The gasification performance, calculated by the Ratio of the upper calorific values of gas to oil and coal, was fraudulent approximately 69%. The total cost of product gas compression is 20,800 KW upon delivery below 15 ata each 17.9 109 Kcal / d.

Example II The procedure in Example I is essentially repeated, however, the coal above the upper phase boundary of the fluidized bed in introduces the carburetor, the gasification at a temperature of 871 0C and a pressure of 14 ata and 50% by volume of that introduced below the fluidized bed Steam replaced by recycle gas, so that from the gasifier a gas product with a Methane content of 7 vol .-% (25% of the carbon in the product gas) emerges. In In this particular example it is not necessary to have the steam through to any significant extent To replace recycle gas, since according to Example I a small amount of steam was used.

Example III The procedure of Example I is essentially identical repeated, however, the finely divided coal using a carrier gas from 50 vol .-% steam and 50 vol .-% air is pneumatically conveyed to the gasifier. This coal-like flow contains 20.8 kg of coal per m3 of carrier gas the actually prevailing conditions. The carbon-containing carrier gas has at the Mix a temperature of about 204 ° C and a pressure of about 9.8 ata or about 0.5 ata more than the pressure around the carburetor. The carrier gas will the pneumatic system, i.e. on the upstream side in line 25, with a pressure of 12.6 ata fed. In the pneumatic delivery system there is a pressure drop of 3 at maintained. The nozzle 31 is with 906 kg / h of low pressure steam cooled and kept at a temperature of 204 0C, so that inadmissible agglomeration finely divided coal is avoided. The nozzle 31 is directed downward, and the coal solids become about 61 cm below the center of the dense fluidized bed thrown off the upper interface.

Examples IV to VIII The procedure of Example III was in essentially repeated, but with the carrier gases specified below instead of the carrier gas used in Example I were used: Example carrier gas IV Recycle Product Gas V Carbon Dioxide VI Nitrogen VII Steam VIII Air Example IX Referring to Fig. 2, a specific example of the production of heating gas according to the invention indicated, but the invention does not restricts. The gas from the gasification part is up to form a fuel gas Desulfurized to a maximum content of 100 ppm total sulfur. This low sulfur content is made by a combination of carbon oxysulfide hydrolysis and hydrogen sulfide removal achieved. The alkazide method is used to remove hydrogen sulfide. The concentrated hydrogen sulphide stream from the regenerator for the alkazide solution, elemental sulfur is set in a Claus plant.

In particular, the gas from the gasification becomes steep in the compressor 102 compressed to a pressure of about 5.6 at. Gas compression is only required when the carburetor is operated at a pressure less than that required Delivery pressure is. The compressors are driven by a steam turbine, whereby some of the drive steam is blown off and the rest is condensed. The one in that Waste heat branch of the gasification generated reaction steam of 84 at and 5100C is on the required feed pressure for the carburetor expands. The remaining energy will supplied by condensation of the vapor of 84 at and 5100C at 152 torr. Of the Compressor, the gas is delivered to the catalytic hydrolysis unit 104, where the Most of the carbon oxysulphide with the water contained in the presence of activated Aluminum oxide or cobalt / molybdenum catalyst with the formation of hydrogen sulfide and carbon dioxide is converted. The feed gas temperature is determined by heat exchange with the hot hydrolysis exhaust gases in the heat exchanger 106 to the hydrolysis temperature, e.g. about 121 to 1770C. The exhaust gases from the hydrolysis are through the Air cooler 108 and finally further cooled by the water cooler 110 to about 380C. The final cooling to the temperature required for the alkazide absorber, i.e., about 21 ° C, is passed through refrigeration plant 112.

In the alkazide absorber 114, the hydrogen sulfide is through the Alkazide solution, an aqueous solution of the potassium salt of Dimethylaminoacetic acid, selectively absorbed. The alkazide process selectively absorbs hydrogen sulfide in the presence of carbon dioxide, so that a more concentrated hydrogen sulfide feed often with around 20% by volume of hydrogen sulfide for the Claus plant. The consumed Solution from the absorber is generated by expelling with low-pressure steam in a digester degasser 118 regenerated at about 104 to 127 ° C under a pressure of about 0 to 0.7 at. The heat exchange in exchanger 116 between the used and regenerated Solution reduces the amount of low pressure steam required in the cooker degasser. The overhead gases from the alkazide absorber contain less than 100 ppm sulfur and are released as heating gas.

Example X The procedure of Example IX essentially followed repeated, but to generate a fuel gas with low or medium Calorific value in the gasifier instead of air an oxygen-enriched air was used.

Example XI The procedure of Example IX essentially followed repeated, but to generate a fuel gas with a medium calorific value in oxygen was used in the carburetor instead of air.

In summary, the invention relates to a process for continuous, simultaneous gasification of liquid and solid carbonaceous material one in carbon monoxide, hydrogen and, if desired, methane rich product by selective introduction of the liquid, carbonaceous material into a fluidized bed formed by the solid carbonaceous material. The gasification is carried out in a gasifier, which has a lower, dense fluidized bed from the solid material and one adjacent to the upper phase boundary of the bed contains upper, dilute, discharged particles containing gas zone. The liquid, carbonaceous material is near the upper phase boundary in the gasifier introduced. It reaches the upper phase boundary of the fluidized bed and comes with it the surface of the solid material in the fluidized bed serving as the reaction site in contact. The liquid material is quantified so that in the carburetor the gas generation is increased.

Claims (35)

P atent claims 1. Process for continuous simultaneous Gasification of liquid and solid carbonaceous material with an oxygen containing gas and water vapor to a rich in carbon monoxide and hydrogen Gas in a gasifier with one fluidized bed of the solid material and one above of the fluidized bed located gas phase at a: 4 maximum temperature in the area from about 816 to 13160C, dgd. the liquid material is close to the upper phase boundary of the Introduces fluidized bed into the gas phase and a substantial portion of it in liquid Applies form to this phase boundary. 2. The method according to claim 1, dgd. you put the liquid material on a Temperature in the range of ambient temperature to 4270C at which the Implementation begins, but thermal cracking on the way to the gasifier is avoided will. 3. The method according to claim 1 or 2, dgd. one the solid, carbonaceous one Material under a pressure higher than the carburetor pressure illit a temperature in the range from ambient temperature to 5380C in such an amount into the carburetor introduces that the upper phase boundary of the fluidized bed is kept at a given height is, the ratio of the heights of the gas phase and the fluidized bed in the area from about 3: 1 to 10: 1. 4. The method according to any one of claims 1 to 3, dgd. one the oxygen containing gas with up to 50 vol .-% steam with an average overall temperature of up to about 5380C. 5. The method according to any one of claims 1 to 4, dgd. at least one about 40 wt .-% of the steam at the lower phase boundary of the fluidized bed with a Temperature of up to about 6490C in such an amount that the lower Area of the bed is whirled up. 6. The method according to any one of claims 1 to 5, dgd. one in the fluidized bed with a temperature below the softening temperature of the ash of the solid or liquid material works. 7. The method according to any one of claims 1 to 6, characterized in that that the solid material is coal and the liquid material is a liquid hydrocarbon is that the carburetor pressure under excess pressure, preferably above about 1.5 ata, holds, the gaseous reaction product pass into the gas phase and with a considerably higher empty pipe speed than the point of the beginning whirling up corresponds to and up to about 6.1 m / s with a residence time in the gas phase of about Allow 2 to 50 seconds to flow through the gas phase. 8. The method according to any one of claims 1 to 7, characterized in that that you can put the coal directly in and under the top Phase boundary of the Fluidized bed in the carburetor introduces V I 'the pressure in the carburetor in the area from about 2 to 30 ata, preferably in the range of about 6 to 14 ata. 9. The method according to any one of claims 1 to 8, characterized in that that the temperature in the fluidized bed is in the range of about 927 to 12050C. 10. The method according to any one of claims 1 to 8, characterized in, that one can produce a product gas with a higher methane content for methane formation applies favorable conditions, preferably the solid material above the above Phase boundary of the fluidized bed in. Introduces the gasifier. 11. The method according to claim 10, characterized in that at Temperatures of about 815 to 9270C will work. 12. The method according to claim 10 or 11, characterized in that one works at a pressure of at least about 10 ata and the amount of steam used reduced rather than replaced by recycle gas. 13. The method according to any one of claims 7 to 12, characterized in that that you get the liquid hydrocarbon at a rate in the range sprays from about 6.1 to 30.5 m / s onto the upper phase boundary of the fluidized bed. 14. The method according to any one of claims 7 to 13, characterized in that that one introduces the liquid hydrocarbon in the form of spray droplets. 15. The method according to any one of claims 7 to 4, characterized in that that the liquid hydrocarbon in the form of spray droplets of a size in in the range of about 10 to 500 zu. 16. The method according to any one of claims 1 to 15, characterized in that that the coal is in particulate form in a size in the range of 0 to about 9.5 mm a carrier gas at a temperature from ambient up to about 5380C in an amount of about 3.2 to 32 kg per m3 of carrier gas under the prevailing conditions gives up and thus pneumatically conveyed into the carburetor. 17. The method according to any one of claims 1 to 16, characterized in that that the upper phase boundary of the fluidized bed is about 1.2 to 6.1 m above the lower phase boundary holds. 18. The method according to any one of claims 1 to 17, characterized in, that one has the oxygen-containing gas and at least about 50% by weight of the steam under a pressure slightly above the carburettor pressure at spatially separated, substantially evenly distributed over the circumference points in the fluidized bed introduces, the introduction of the oxygen-containing gas in different Heights he follows. 19. The method according to any one of claims 1 to 18, characterized in, that additional proportions of the oxygen-containing gas with up to about 10 vol .-% Steam at or just above the boundary between the fluidized bed and the gas phase at spatially separated, essentially evenly distributed points over the circumference in such amounts that they with the fluidized bed forming carbon carriers react, increase the temperature of the dilute phase and the carbon turnover performance improve the process, resulting in a crude product gas that at least contains about 50% of the oxidized carbon in the form of carbon monoxide. 20. The method according to any one of claims 1 to 19, characterized in that that you get the gaseous reaction product with a significantly higher superficial velocity than corresponds to the point of the beginning of the whirling up and with up to about 6.1 m / s with a residence time in the gas phase of about 2 to 50 seconds through the gas phase lets flow, with further gasification occurs and the gas phase on one with the Properties of the contained ash agree maximum temperature is maintained. 21. The method according to any one of claims 1 to 20, characterized in that that one generates the product gas under selective conditions, so that the formation undesirable, heavier hydrocarbons as by-products to a minimum limited remain. 22. The method according to any one of claims 1 to 21, characterized in that withdrawing the crude product gas from the upper dilute zone up to about 60% by weight of the partially consumed coal is withdrawn from the bottom of the fluidized bed and for the purpose of recovering sensible heat and steam preheating with at the lower phase boundary brings into contact steam introduced into the fluidized bed. 23. The method according to any one of claims 1 to 22, characterized in that that the crude product gas in a heat recovery zone to temperatures of about 93 to 2600C cools and substantial amounts of partially consumed coal for the purpose of removal from the process or recirculation or work-up from the product gas removed to a content of less than about 141 solid particles per Nm3 and utilizes the recovered heat to generate steam, part of which is in the Process is recovered. 24. The method according to any one of claims 1 to 23, characterized in that that one in the heat recovery zone under the prevailing there, below The pressures lying below the gasifier pressure cooled product gas through a high-performance scrubber conducts with a high pressure drop, removing fine, partially used coal particles and a product gas containing less than about 3.5 solid particles each Nm3 gas, at least about 10% by volume carbon monoxide, at least about 10% by volume hydrogen and with a calorific value of at least about 800 Kca-l / Nm3 and the carburetor pressure by back pressure control on the gas system on a downstream side of the carburetor is under overpressure, preferably under pressure above holds about 1.5 ata. 25. The method according to any one of claims 1 to 24, characterized in that that you keep the maximum temperature in the carburetor at about 927 to 12050C, the Raw product gas has about 55 to 85% of the oxidized carbon in the form of carbon monoxide and the scrubber is a venturi scrubber which has a product gas with less than delivers about 0.35 solid particles per Nm3 gas. 26. The method according to any one of claims 1 to 25, characterized in that that the ratio of height to maximum diameter of the fluidized bed in the area from about 1: 2 to 5: 1. 27. The method according to any one of claims 1 to 26, characterized in that that the cooled product gas has less than 3.5 solid particles per Nm3 gas used as a raw material for the production of heating gas. 28. The method according to any one of claims 1 to 27, characterized in, that the oxygen-containing gas is air or air enriched with oxygen and the cooled product gas containing less than 0.35 particulate matter per Nm3 of gas as the starting material for the production of heating gas with a low calorific value begins. 29. The method according to any one of claims 1 to 27, dadurdt gweZenn- < draws that the oxygen-containing gas is oxygen or oxygen-enriched Is air and one is the cooled product gas with a content of less than 0.35 solid particles per Nm3 as the starting material for the production of a heating gas with a medium calorific value begins. 30. The method according to any one of claims 1 to 27, characterized in, that the particulate solid carbonaceous material at or below the upper limit of the fluidized bed introduces into the gasifier, as containing oxygen Gas supplies oxygen and the cooled product gas with less than 0.35 solid particles uses per Nm3 of gas as a starting material for the production of methanol. 31. The method according to any one of claims 1 to 27, characterized in that that the solid carbonaceous material is at or below the upper limit introduces the fluidized bed into the gasifier and the cooled product gas with a Content of less than 3.5 solid particles per Nm3 gas as starting material for the Production of ammonia begins. 32. The method according to any one of claims 1 to 29, characterized in that that the cooled product gas has less than 3.5 solid particles per Nm3 gas and a content of carbon oxysulfide and hydrogen sulfide in a desulfurization zone introduces, there in a first phase carbon oxysulfide in the presence of a carbon oxysulfide hydrolyzing catalyst with the formation of hydrogen sulfide and from the hydrolysis product gas containing increased amounts of hydrogen sulfide in a second phase with the formation of a desulphurised hydrogen sulphide heating gas absorbed. 33. The method according to claim 32, characterized in that the Carries out hydrolysis under a pressure of more than 4.2 ata. 34. The method according to claim 32 or 33, characterized in that one the hydrolysis at a temperature of about 93 to 204 0C and the hydrogen sulfide absorption at a temperature of 21 to 380C and a pressure of more than about 4.2 ata. 35. The method according to any one of claims 1 to 34, characterized in that that the liquid material in an amount of 0.01 to 20 kg per kg of in the Carburetor imported solid material.