DE2728437A1 - METHOD AND DEVICE FOR THE PYROLYSIS OF CARBONATED MATERIAL - Google Patents

Description

Occidental Petroleum Corporation, 10889 Wilshire Boulevard, Los Angeles, California 90024 - U.S.A.

Method and device for the pyrolysis of carbonaceous material

The invention relates to a method for the pyrolysis of solid carbonaceous material by acting on this material Heat transmitted from a particulate heating source, with a carbonaceous particulate residue as a pyrolysis product obtained and the particle heating source formed by oxidation of at least a portion of the solid-containing solid particle residue is and a device for performing the method.

The growing scarcity of liquid fossil fuels,

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709881/0981

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ROEHMERT & BOEHMERT

such as oil and natural gases, draws attention to the conversion of solid carbonaceous materials, such as Coal, oil shale, tar sands, glisonite and solid waste turn into liquid or gaseous hydrocarbons Set up pyrolysis. Pyrolysis can be carried out under non-oxidizing conditions in a pyrolysis reactor in the presence of a Particle heat sources take place, resulting as products pyrolytic vapors, the hydrocarbons and Contain carbonaceous particulate matter residues. The particle heating source for carrying out the pyrolysis of carbonaceous Material can be produced by oxidation of carbon in the carbonaceous particulate matter residue in a combustion chamber be generated.

With the use of a combination of pyrolysis reactor and combustion chamber to obtain hydrocarbons from carbonaceous solid materials are many problems tied together. One of these problems is coal sticking along the walls of the pyrolysis reactor when that carbonaceous material is agglomerated coal, especially in the case of Eastern American coal (Eastern United States coal), which, as experience shows, has a tendency to agglomerate in a reactor, especially along the walls.

Another problem concerns the transfer of the carbonaceous Particulate matter product from the pyrolysis reactor to the combustion chamber while at the same time preventing is that oxygen present in the combustion chamber enters the pyrolysis reactor. When oxygen is in the If the pyrolysis reactor penetrates, the value of the hydrocarbon products is reduced; also can be violent Explosion occur.

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BOEHMERT & ßOEHMERi

A third problem relates to the need to maximize the production of carbon dioxide in the combustor and to minimize the production of carbon monoxide in order to recover the calorific value of the carbonaceous solid residue to maximize during oxidation. The kinetic and thermodynamic equilibria of the oxidation of Carbon favor an increased production, of Carbon monoxide in relation to carbon dioxide at temperatures above about 1200 ° F (650 ° C) for long residence times when there is a stoichiometric oxygen deficit. Because the pyrolysis of carbonaceous material is often carried out at temperatures above 1200 F (650 C) and Can reach temperatures above 2000 F (1100 C), it is necessary to design a particle heating source whose Temperatures higher, often considerably higher, than 1200 ° F (650 C) are. Furthermore, the carbon-containing solid particle residue becomes in the case of a stoichiometric oxygen deficit only partially oxidized to form the particle heating source. Hence the production of carbon monoxide occurs inevitably during the oxidation of the carbon-containing solid particle residue. The resulting carbon monoxide forms a loss factor for the thermal effectiveness of the procedure.

The invention is therefore based on the object of creating a method and a device of the type mentioned at the beginning, which when a carbonaceous particulate pyrolysis residue the carbonaceous material is oxidized to provide a particulate heating source for pyrolysis of the carbonaceous material to form, prevents oxygen from entering the pyrolysis reaction and at the same time the production of carbon dioxide is maximized while the production of carbon monoxide is minimized, increasing levels of carbonaceous Solid material can be obtained by pyrolysis, which are useful with agglomerated coal.

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BOEHMERT & BOEHMERT

The solution to this problem is provided according to the invention that at least part of the carbonaceous material obtained by pyrolysis Solid material formed carbonaceous solid residue is brought to a fluidized bed surrounding a substantially vertically directed open tube, the Tube is in open connection with a substantially vertically directed riser pipe and the tube and the Riser pipe form a first combustion chamber; that the solid residue from the fluidized bed into the first combustion chamber by blowing a gaseous source of oxygen up the tube is led to carbon in the solid residue to the partial Heating the solid residue to oxidize and around the solid residue and gaseous combustion products of the solid residue, including carbon monoxide, of a second combustion zone to feed; and that an oxygen source of the second combustion zone in a proportion of at least 50% of the molar supply the carbon monoxide is fed to the second combustion zone, so that all of the oxygen supply to the first and second Burning zone is sufficient to generate the particle heating source.

A preferred embodiment of the invention stands out characterized in that the tube is spaced from the riser pipe; and that the carbonaceous particulate residue in the Fluidized bed is whirled up by an upward flow of a fluid gas which zv / ischen into the riser pipe through the space enters the riser and tube. The flowing gases desirably contain oxygen.

Another preferred embodiment of the invention provides that the carbonaceous solid material undergoes flash pyrolysis through continuous transport of the carbonaceous Particulate matter feed contained in the carrier gas is, essentially not with respect to the pyrolysis products

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is deleteriously reactive, to a vertically directed, downward flow provided pyrolysis reactor is exposed, wherein the pyrolysis reactor contains a pyrolysis zone, which at a Temperature below about 2000 F (1100 C) operates; that the particle heating source at a temperature above the The pyrolysis temperature is fed to the pyrolysis reactor at a rate sufficient to keep the pyrolysis zone at the pyrolysis temperature to keep; that a turbulent mixture of particle heating source, the carbonaceous particulate matter feed and forming the carrier gas to pyrolyze the carbonated solids feed and a To obtain pyrolysis product stream, the particle heating source as solids and a carbon-containing solid pyrolysis residue contains as well as a vapor mixture of the carrier gas and the pyrolysis vapors consisting of hydrocarbons exist; and that the pyrolysis product stream from the pyrolysis reactor passes into a first separation zone, thus at least the The bulk of the solids are separated from the steam mixture.

Another preferred embodiment of the invention provides that the first separation zone is a cyclone separation zone.

Further preferred embodiments of the invention are characterized in that the one formed by the second combustion zone Particle heating source and the gaseous combustion products are separated from one another in a cyclone separation zone, or alternatively, that the second combustion zone forms a cyclone oxidation separation zone.

According to a particularly preferred embodiment of the invention Process is provided that the pyrolysis reactor has a solids inlet for the carbonaceous solid material feed and a vertically arranged chamber surrounding the upper part of the pyrolysis reactor, the inner

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Circumferential wall of the chamber an overflow weir to a vertical one directed mixing zone of the reactor forms; that the carbon sotff-containing solid particle material in a carrier gas transported to the solids feed inlet and there in the Mixing zone is blown in; that the particle heating source is led to the vertically directed chamber and in the chamber swirled around by the flow of the flowing gas, which is essentially non-detrimentally reactive with respect to the pyrolysis products will; that the swirled particle heating source is discharged over the weir and down into the mixing zone to create a turbulent Mixture with the particulate carbonaceous material to build; and that the mixture passes downward through the mixing zone to the pyrolysis zone of the pyrolysis reactor, to the to pyrolyze carbonaceous solid material.

To carry out the method according to the invention is a Apparatus for forming a particulate heating source from a carbonaceous particulate pyrolysis residue of the carbonaceous material for pyrolysis of the carbonaceous Solid material provided, which is marked is through a container for receiving a fluidized bed of the carbonaceous solid particle residue of the pyrolysis around an open, substantially vertically directed tube; through an essentially vertically directed riser in open connection with the riser pipe; Introducer for introducing the carbonaceous solid particle residue pyrolysis in the fluidized bed; Injection means for injecting a gaseous source of oxygen upwardly into the tube for transferring the carbonaceous residue from the fluidized bed into the tube; and supply means for supplying additional oxygen to the combustion chamber to form the particle heating source.

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BOEHMIZKT & RORHMEKT

Such an apparatus is particularly useful in connection with a pyrolysis reactor having a particle heating source uses. Therefore, a preferred embodiment of the present invention is characterized by a Pyrolysis reactor with downflow; by means of forming a turbulent mixture of the particle heating source and the solid carbonaceous material contained in a carrier gas for introduction into the pyrolysis reactor for pyrolysis of the carbonaceous solids feed are included to to form a pyrolysis product stream comprising a vapor mixture and, as solids, the particle heating source and a Contains carbonaceous solid residue from pyrolysis; by a first separator for separating at least the majority of the solids from the vapor mixture in the pyrolysis product stream; by transfer means for transferring the pyrolysis product stream from the pyrolysis reactor to the first separator; by means for forming the particle heating source emerging from a container consist of a fluidized bed of the separated solids around an open, essentially vertically directed riser pipe in open connection with the tube, a combustion chamber in connection with the riser pipe, supply means for supply a gaseous source of oxygen up the line for entraining the solids from the fluidized bed into the line and contains means for supplying oxygen to the combustion chamber, to heat the solids and form the particle heating source; by means of transmission for the transmission of the Fuels from the first burner to the fluidized bed; by means for transferring the particle heating source from the second combustion chamber to a second separator; by a second separator for separating the particle magnetic source from the gaseous combustion product; and by means for transferring the separated particle heating source from the second separator to the pyrolysis reactor.

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BOEMMERT & BOEHMERT

Other embodiments of the invention provide that the The tube is separated from the riser and that the separator is a cyclone separator and that the second separator is a cyclone separator is.

Another, extremely preferred embodiment provides that the second combustion chamber and the second separator are integrated as a cyclone oxidation separator.

According to a preferred embodiment of the present invention it is further provided that the pyrolysis reactor has a substantially vertically directed mixing zone and a substantially vertically directed pyrolysis zone; that the pyrolysis reactor has a solids feed inlet, a substantially vertically arranged chamber surrounding the upper part of the reactor and an inner peripheral wall owns an overflow weir to the vertically directed Mixing zone forms; and that the means for forming a turbulent mixture is supply means for supplying the particle heating source keep in a flowing state; and that injecting means for injecting the im from the solids supply inlet Introduced into the mixing zone carrier gas contained carbon-containing Solid feed the resulting turbulent Form mixture.

Another, extremely preferred embodiment of the invention is characterized by a pyrolysis reactor with downward directed flow, which is a substantially vertically directed flow Mixing zone, a substantially vertically directed pyrolysis zone, one solids feed inlet and one substantially has vertically directed chamber surrounding the upper part of the reactor, the inner peripheral wall of the Kaironer forms an overflow weir to the mixing zone, in which the

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Agglomerated carbon feed contained in a carrier gas with a Particle heating source under turbulent flow conditions in the pyrolysis zone of the pyrolysis reactor is connected to obtain a pyrolysis product stream, which as solids the particle heating source and a carbonaceous solid contains residual particles from pyrolysis and a vapor mixture; by supply means for supplying the particle heating source to the vertically directed chamber; by introducing means for introducing a flowing gas into the chamber to the particle heating source to keep in a fluid state therein; by transfer means for transferring the coal supply from the solid feed inlet into the mixing zone; through a first cyclone separator in connection with the pyrolysis reactor for separation at least the majority of the solids in the pyrolysis product stream from the vapor mixture in the pyrolysis product stream; by Means for forming the particle heating source consisting of a vessel containing a fluidized bed of the separated solids around an open, substantially vertically directed tube, a substantially vertically directed riser pipe in open connection with the vertically directed tube and separately from a second combustion chamber in connection owns with the riser; by introducing means for introducing a gaseous source of oxygen upwardly into the Tube for entraining the solids from the fluidized bed into the tube and for partially oxidizing the carbon in the solids to heat the solids with additional formation of combustion products; through introducers for the introduction of oxygen into the second combustion chamber for further heating of the solids to the To form particle heating source; through a pipe from the first Cyclone separator to the fluidized bed to transfer the separated Solids from the first cyclone separator to the fluidized bed; by a second cyclone separator in connection with the combustion

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chamber for separating the particle heating source from the gaseous products of combustion; and through a pipe from the second cyclone separator to the chamber surrounding the top of the pyrolysis reactor for the particle heating source to the pyrolysis reactor transfer.

Further advantages and features of the invention emerge from the claims and from the following description, in which an exemplary embodiment is explained in detail with reference to the drawing. It shows:

1 schematically shows the process and one of the processes according to the invention Features owning device; and

Fig. 2 is an enlarged and detailed view

of the area labeled "2" in FIG.

The drawing illustrates a pyrolysis unit 8 with a pyrolysis reactor 10 with downward flow. The pyrolysis reactor 10 has an essentially vertically oriented mixing zone 12 or a mixing area and furthermore an essentially vertically oriented pyrolysis zone 14 or a pyrolysis area below the mixing zone 12. The arrow 16 shows the approximate extent of the pyrolysis zone 14. The pyrolysis reactor 10 has a knee 18 towards the end of the pyrolysis zone 14, by means of which it is held. The lower end 20 of the pyrolysis reactor 10 ends in a separate zone in a cyclone separator 22.

A substantially upright, circular, solid feed inlet 24 terminates in the mixing zone 12 and is at the end narrows to form a nozzle 26. Inlet 24 is adapted to bring solid carbonaceous material into the mixing zone 12 to be introduced.

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The upper end 28 of the reactor 10 is open and of larger diameter than the nozzle 26 ^ creating an annular Gap 30 is formed between the upper end 28 of the reactor 10 and the nozzle 26. A vertically oriented Swirl chamber 3 2 or a container surrounds the top of the reactor 10 and is preferably in a circular shape Section 3 4 is formed of the wall 3 6 of the feed inlet 24 of the solids above the narrowing of the wall 36 to a nozzle 26 and the upper end 28 of the reactor 10 connects. The chamber 32 surrounds the nozzle 26 and a portion of the upper end 28 of the reactor 10. The inner surrounding wall of the chamber 3 2 is through the upper end 28 of the reactor 10 and serves as an overflow weir of the mixing zone 12 of the reactor 10.

A second, vertically oriented inlet 38 for solids preferably ends in the annular vortex chamber 3 2 a point located on a level below the upper edge 40 of the pyrolysis reactor 10.

A gas inlet 42 for a fluidizing gas is located at the bottom of the fluidizing chamber. To distribute the fluidizing gas in such a way that the fluidizing gas flows upwards through the vortex chamber 3 2, are means such as a cylindrical, horizontally oriented, perforated plate 44 is provided which rests against the bottom of the vortex chamber 32 below the end of the second inlet 38 are arranged.

The first cyclone separator 22 serves to remove carbon-containing solid particles remaining from the pyrolysis to separate gaseous pyrolysis product.

The particle heating source for the pyrolysis reactor is through

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Oxidation of at least some of the carbonaceous solid particles remaining in the combustion unit educated. The incineration unit 50 includes a vessel 52 which holds a fluidized bed 60 of carbonaceous particulate matter residue on an open, substantially vertically oriented tube 54 or conduit. A Gas inlet 56 for transporting the gas is located at the base of the container 52. The gas inlet 56 is tapered around a vertically oriented nozzle 58 for injecting the transport gas directly into the open tube 54. The fluidized bed 60 of the carbonaceous solid residue is from a Swirl gas entering the chamber through gas inlet 62 at the base of container 52 flowed. The fluidizing gas is through the fluidized bed 60 by means of a second, horizontally oriented perforated distributor plate 64 distributed.

The upper end 66 of the container 52 tapers upwards and inwards for connection to a vertically oriented one Riser 68. The riser 68 and tube 54 define a first combustion zone or chamber. The riser 68 couples the container 52 to a second combustion zone or chamber 70. The tube 54 lies below the riser 68. The Upper edge 72 of the tube 54 is so far away from the riser pipe 68 that an annular space gap 74 between the Inlet 76 to the riser 68 and the upper edge 72 of the tube 54 is formed. The top 71 of the tube 54 can be inwardly be tapered so that the diameter of the tube 54 at an upper edge 7 2 is narrower than the diameter of the riser pipe 68.

A vertically oriented normal pipe or drop leg 78 with grazing gas inlets 122 extends from the bottom of the

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first cyclone separator 22 into the container 52 below the upper end 80 of the fluidized bed of the carbonaceous Solid residue. Solid particles separated by the first solids separator 22 are separated by the drop leg 78 transferred to the container 52.

An inlet 82 is located in the upper region of the riser 68 for supplying an oxygen source into the second Combustion chamber 70. The second combustion chamber 70 is in open communication with a second separator, such as the cyclone separator 84. This cyclone separator 84 serves to divert the combustion gases present in the combustion unit 50 from the combustion gases in the combustion unit 50 generated particle heating source to separate. The particle heating source is from the second cyclone separator 84 into the second The inlet 38 of the pyrolysis reactor 10 is transferred through a vertical pipe 86 extending from the bottom of the second cyclone separator 8 4 goes out and ends in the second inlet 38. The length of the tube 86 is chosen to accommodate the accumulation of various pressures is compensated for by the backlog of the system. Grazing gas inlets 88 are along the length of the tube 86 is provided.

Overall, a pyrolysis device for solid, carbonaceous Material described, the two main units a pyrolysis unit 8 and a burning unit 50 contains. These both units 8, 50 are through two cyclone separators 22, 84 and two vertically oriented normal pipes or risers 78, 86 connected, which allow the carbonaceous, solid residue, from the pyrolysis unit 8 to the combustion unit 50 transferred to ground, and allow the particle heating source to be transferred from the Varbrennteinhe.it 50 to the pyrolysis unit 8 to become.

In the process according to the invention, a solid particle becomes

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BOEHMERT & BOEHiVIERT

containing carbonaceous material is subjected to flash pyrolysis by the supply of carbonaceous particulate matter contained in a carrier gas through a first supply inlet 24 into the supplying nozzle 26
and is thus transported into the pyrolysis reactor 10. The carrier ice is essentially non-deleteriously reactive with the pyrolysis products and can serve as a diluent to prevent self-accumulation of the carbonaceous material.

Here, under a "non-harmful reactive"
Gas understood a gas stream which is essentially free of free oxygen. Although the gas may contain constituents which react with pyrolysis products under non-oxidizing conditions to increase their valency, the gas should not contain constituents which
Pyrolysis products degrade. The carrier gas can be, for example, the exhaust gas product of the pyrolysis vapor, which reacts under suitable conditions with coal or coke formed by the pyrolysis to produce hydrogen by means of water gas reactions, which is used to react with unsaturated pyrolysis products and to stabilize them; further, any inert gas, or mixtures of these gases are used. The carrier gas can be, for example, a synthesis gas, in particular a synthesis gas enriched with hydrogen.

The carbonaceous material, prior to being fed into the first fluidized bed, can be treated by methods such as removal of inorganic fractions by magnetic separation and classification, particularly in the case of urban solid waste. The carbonaceous material can be dried to reduce its moisture content. The carbonaceous, solid material is usually crushed,

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BOEHMERT & BOEHMERi ¹

to the surface available for pyrolysis enlarge.

Preferably, the substantial proportion of the carbonaceous material is of a particle size smaller than 1000 micrometers in order to form a large surface-to-volume ratio which ensures rapid heating of the coal in the pyrolysis zone. Rapid heating leads to an improved availability of the hydrocarbons. For agglomerated coals, the particle size is preferably primarily below 250 microns, since agglomerated coals are known to soften and stick together at relatively low temperatures, ie 400 to 850 ° F (200 to 45 ° C). Agglomerated coal should therefore be heated quickly through this plastic state before it touches the walls of the pyrolysis reactor in order to prevent it from sticking to the reactor walls. Since the rate at which coal particles can be heated increases as the particle size decreases, it is important that, depending on the size and shape of the pyrolysis reactor, agglomerated coal be reduced to 250 micrometers or smaller so that essentially all of the coal particles are plastic state and have not become sticky when the carbon particles graze the reactor wall. For example, if a bituminous high volatile C-coal which is plasticized at temperatures above 500 ⁰ F (26O ° C) (250 mm) diameter at a temperature of 1075 F (580 C) in a pyrolysis reactor with 1O inch in FIG. 1 If the type shown and described below is pyrolyzed, the carbon should be reduced to a size less than micrometers in diameter to prevent sticking to the reactor walls. Coal particles larger than 250 microns in diameter can

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graze the reactor wall before going through the plastic state.

The carbon-containing one introduced into the pyrolysis reactor Material is preferably free of fine particles with a diameter of less than 10 micrometers because of the There is a tendency for the pyrolysis of the carbonaceous material to leave fine, carbonaceous solid residues have to be carried into and contaminate the liquid hydrocarbon products.

Simultaneously with the introduction of the carbonaceous feed, a particulate heating source is fed into the vortex chamber 32 through the second, vertically oriented inlet 38. Since the preferred embodiment of the second inlet 38 terminates below the top edge 40 of the pyrolysis reactor 10, the particle heating source in the vortex chamber 32 builds up below the weir 28 to form a solid compression. The particle heating source is maintained in a fluidized state in the chamber 32 by introducing a fluidizing gas stream through the gas inlet 42. The fluidizing gas is distributed through the distribution plate 44 to maintain the heat source of the particles in a fluidized state throughout the chamber. With further supply of the particle heating source into the chamber, the particle heating source is guided via the upper end of the weir and through the opening 33 between the weir and the nozzle 26 into the mixing zone 12 of the pyrolysis reactor 10 with the aid of the fluidizing gas. An advantage of this weir-like design is that a substantially constant FIuD of the fluidized particles of the particle heating source enters the mixing zone 12, since the mass of the particle heating source is de behind the weir. ^c ; Reactor is held up and attenuates minor fluctuations in the flow of the particle heating source.

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nor ·} iMHUT & boehmkkt

In the mixing zone 12 of the pyrolysis reactor 10, the im Carrier gas containing carbonaceous material is discharged from the nozzle 26 as a fluid jet 112 which opposes expands the reactor walls at an angle of about 20 or less as shown by dashed lines 88 ' which represent the edge of the fluid jet. When the particle heating source is within the mixing zone 12, it enters the path of the fluid jet 112 of the carbonaceous Material supply flow and carrier gas, which comes from the nozzle 26 and is driven such that a resulting turbulent mixture of the particle heating source, the carbonaceous solid particulate material feed and the carrier gas arises. The fluid stream 112 has a free core area 113 of carbonaceous Material, as indicated by the V-shaped dashed line 114, the core extends considerably into the reactor. Since the fluid jet 112 expands, the existing particle heating source is mixed with the carbonaceous material in the part of the fluid jet 112 drawn around the free core area 113. The particle heating source along the perimeter 88 'of the fluid jet 112 preferably heats the carbonaceous material, in the case of agglomerated carbon, to a temperature above the temperature at which the coal is sticky. In the area 116 between the reactor walls and the fluid jet 112 is an unswept particle heating source (i.e., particulate heat transfer medium).

This mixing of the particle heating source with the carbonaceous solid material in the mixing zone 112 is initiated a heat transfer from the particulate heating source to the carbonaceous material, thereby pyrolysis in the Pyrolysis zone 114 of the pyrolysis reactor 110 is effected.

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BOEi IMERT & BOEIHMI-RT

Pyrolysis is a combination of evaporation and a decomposition reaction. When the evaporation and the decomposition reaction occur, the carbonaceous Material condensable and non-condensable hydrocarbons with an accompanying production of carbon-containing solid residues such as coke or coal or semi-coke generated. The actual pyrolysis time is below about 5 seconds and preferably by 0.1 to 3 seconds to maximize the yield of middle distillates. Middle distillates are the at Medium-temperature boiling hydrocarbons, i.e. Ct - hydrocarbons that have a boiling point of about 95O ° F (510 ° C). These are hydrocarbons useful for making gasoline, diesel oil, heating oil and the like.

The term used "pyrolysis time" means the time from when the carbonaceous material with the Particulate heat source comes into contact until the point in time at which the pyrolytic generated by the pyrolysis Vapors from the particle heating source are separated in the first separation zone, as described below.

A suitable measure of the pyrolysis time is the mean residence time of the carrier gas in the pyrolysis zone 14 of the pyrolysis reactor 10 and the first separator 22. A sufficient one There must be pyrolysis time in order to heat the carbonaceous material to the pyrolysis temperature.

An advantage of the pyrolysis reactor 10 shown in the drawing is that the turbulent flow causes rapid heating the carbonaceous feed, which improves the yield. In the case of agglomerated coal

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there are accumulations of coal particles on the reactor walls prevented by the rapid heating and the turbulent flow. Preferably the particle heating source occurs into the mixing zone 12 in a sub-turbulent Flow rate and the carbonaceous solid material into the mixing zone 12 through the nozzle 26 under turbulent flow conditions one at a rate high enough that that resulting from the two inlet streams Electricity is turbulent. Turbulent flow creates intimate contact between the solid, carbonaceous ones Material and the particles of the particle heating source, causing rapid heating of the carbonaceous Material is achieved. In the case of agglomerated coal, the turbulence causes mixing of the particle heating source with the coal particles in the inner part of the fluid jet 112, with rapid heating of these coal particles takes place through the sticky-plastic state. The term "turbulent" as used means that the flow a flow index Reynolds number greater than 2000 based on the calculation at carrier gas velocities owns under operating conditions. Laminar flow in the pyrolysis reactor 10 tends to be a serious limitation the heat transfer rate within the pyrolysis zone 14. The process parameters, such as the nozzle diameter and the mass flow rate of carbonaceous material and the carrier gas, are varied to increase the rate of flow of the through the first inlet into the turbulence region to maintain incoming particle flow.

The end of the solids supply inlet is preferred cooled, for example by water, if agglomerated carbon is pyrolyzed, otherwise by heat transfer from the surrounding the end of the solids feed inlet

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Particle heating source the inlet is heated above the point which makes the coal sticky.

Although the drawings have a solids supply inlet 24 iii a nozzle 26 at its end in order to obtain high inlet velocities into the mixing zone is a nozzle-like inlet not required. Alternatively, the carbonaceous material and its carrier gas can be included at a sufficiently high velocity to inlet 24 so that the resulting mixture is in a vortex flow is present without the need for a nozzle.

The hot particulate heating source is single-pass srate and fed to a temperature that is compatible with maintaining a temperature for pyrolysis in the Pyrolysis zone is compatible. Pyrolysis starts at around 600 F (315 C) and can go up to temperatures above 2000 ° F (1100 ° C). Preferably the However, pyrolysis is carried out at temperatures ranging from about 900 F (84 ° C) to about 1400 ° F (76O ° C) to achieve the yield of mid-boiling hydrocarbons. In contrast, higher temperatures are favorable Gasification reactions. The maximum temperature in the pyrolysis reactor is limited by the temperature at which the inorganic portion of the particle heating source or the carbonaceous one Material soften with the result of fusing or slagging.

The weight ratio depends on the pyrolysis temperature The particle heating source to the carbonaceous material is preferably in the range of 2 to 20 am Input of the reactor. With conditions in this area the particle heat source in the reactor at a temperature

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temperature from about 100 to about 500 ° F (55 to 280 ° C) above introduced the desired pyrolysis temperature.

For reasons of economy, the amount of maintaining the vortex gas injected into the vortex chamber as low as possible, the inlet 42 is determined by the condition that the particle heating source is kept in a vortex state. Preferably at least a portion of the fluid gas is admitted into the mixing zone of the reactor in order to countercurrent formations to prevent the resulting backmixing of partially used particle heating source. The amount of the carbonaceous solid material introduced carrier gas is such that a turbulent flow occurs during the advancement of the carbonaceous solid material Solid material is maintained by the plastic state in the case of agglomerated carbon. Sufficient Carrier gas must be introduced to prevent undesirable pressure fluctuations due to flow instabilities. The one used to transport the carbonaceous solid material The proportion of gas used is sufficient to prevent clogging in the reactor and is normally higher the amount at which the solid material dilutes and prevents self-clumping in the case of agglomerated carbon will.

In general, a high solids content in the pyrolysis feed stream is desired in order to accommodate the facility size and minimize costs. However, the resulting turbulent mixture contains enough carrier gas that the Mixture has a solids content in the range of about 0.1 up to about 10% of the volume based on the total Stromvoluraens owns to rapid turbulence

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To ensure heating of the carbonaceous material, to dilute the carbonaceous material and to to help prevent self-clumping, especially when working with agglomerated coal. Fast Heating leads to a high yield and prevents the agglomerated carbon from sticking.

The size and configuration of the pyrolysis reactor will chosen so that the desired residence time of the pyrolysis reaction is maintained. When the pyrolysis temperature is reduced, longer residence times are generally used in order to achieve the desired yield of to obtain volatile hydrocarbons.

For reasons of economy, the pressure is in the pyrolysis reactor typically above atmospheric pressure to compress the vapors formed during pyrolysis, so that low volume separation equipment can be used downstream of the reactor.

A pyrolysis product stream grazes the end 20 of the pyrolysis reactor 10 to the first cyclone separator 22. The pyrolysis product stream contains solids, the particle heating source and the carbonaceous solid particles resulting from pyrolysis arise, and a vapor mixture of carrier gas and pyro-Iytic Gases containing non-condensable hydrocarbons. The first cyclone separator is preferably stationary 22 in open connection with the lower end 20 of the pyrolysis reactor 10, so that a quick separation of the vapors from can be carried out on the solids to minimize the pyrolysis time so that the vapors can be cooled, in order to prevent splitting reactions occurring, which reduce the yield of middle distillates from the pyrolytic

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BOEHMERT cSi BOEHMERT

Try to reduce steam. In the cyclone separator 22 is at least the bulk of the solids separated from the steam mixture. The steam mixture contains pyrolytic Vapors that contain volatile carbons, inert carrier gases, and other than hydrocarbon components, such as hydrogen sulfide, which is generated in the pyrolysis reaction can be.

The volatile hydrocarbons produced in pyrolysis consist of condensable carbons that are produced by contacting volatile hydrocarbons such as methane Can be recovered and other hydrocarbon gases that cannot be obtained by common condensing agents are recoverable. Condensable hydrocarbons can be released indirectly by conventional means such as venturi wet cleaners Heat exchangers, washing towers and the like separately and to be recovered. Unwanted gaseous products can come from the uncondensable hydrocarbons for example can be removed by chemical sprinkling. Residual uncondensed hydrocarbons can are sold as a gas product and can be used as a carrier gas to carry the carbonaceous material into to carry the pyrolysis reaction zone.

The particle heating source is formed in the combustion chamber 50. The solids separated in the first cyclone separator 22 fall through tube 78 into fluidized bed 60 which contains the spent particulate heating source and carbonaceous solids contains pyrolysis. When the solids fall through the pipe, the hydrocarbons are on the surface the solids are stripped off by an upward flow of stripping gas that is non-deleteriously reactive with respect to the pyrolysis products, such as steam.

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The stripping gas is through a gas inlet 120 to the Side of the tube 78 fed. The fluidized bed 60 is in a fluidized state by an upward flow of a fluidizing gas stream 91 held in the container 52 through the gas inlet 62. The fluidizing gas flow is through the distributor plate 64 distributed. The fluidizing gas can be non-reactive with respect to the solids in the fluidized bed 60, for example be a degassing product of pyrolysis or the gas may contain some of the oxygen required for oxidation of the solids is required to the particle heating source to build.

A transport gas is introduced up into the riser pipe 54 through the gas inlet 56 and the nozzle 58. The transport gas preferably contains free oxygen. Other reactants that lead to the formation of carbon monoxide may be present. These include steam and carbon dioxide. When steam is present, hydrogen is also formed.

In the preferred process, as noted, the transport gas contains some oxygen to generate some heat, which is necessary to raise the coal to the temperature required for supply to the pyrolysis reactor in the first combustion zone is required. However, the oxygen content is limited because if there is too much oxygen in the transport gas, the carbon monoxides generated in the transport passage cannot be converted into carbon dioxide in the second combustion zone without too much additional oxygen being introduced into the second combustion zone which is above the temperature is, which is required for feeding to the pyrolysis reactor.

As indicated in Figure 1, the transport gas may be a stream of air 90 passing upwardly through the gas inlet 56 and the nozzle

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is passed into the tube 54. Sufficient intake this air stream 90 with an appropriate proportion of oxygen is maintained to remove solids from the fluidized bed 6O to pull out into line 54 so that part of the carbon obtained in the solids is oxidized to add the carbons in line and tube 54 heat, and up around the solids and combustion products of the solids, including carbon monoxide to be transported through the vertical riser pipe 68 into the second combustion chamber 70. The fluidizing gas stream 91 passes through a circular, or spatial, gap 74 between the upper edge 72 of the conduit and the vertical riser 68 to help entrain the solids up into the second combustor 70. If the upper part 71 of the Conduit is narrower in diameter than the riser 68, the gas and solids flow up the tube 54 can in the riser 68 serve to draw the vortex gases into the riser 68 through the annular gap 74.

The velocity of the transport gas is kept high enough to draw the solids into the line and transfer them to the second burning zone. For example, if the transport gas contains air as a source of oxygen, can be a substantially free oxygen-free diluent gas such as nitrogen or flue gas be combined with the air to form an oxygen-lean Maintain carrier gas at a sufficiently high velocity to entrain and transport the solids, without introducing too much oxygen to produce too much carbon monoxide. By diluting the heated air stream A carrier gas stream is formed which contains less than 20% by volume of oxygen.

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The amount of oxygen in the transport gas is controlled so that the desired temperature at the riser pipe 68 is maintained. This amount is always below the stoichiometric amount required for complete oxidation of the coal. Because of this oxygen deficit and the relatively high temperature in the riser, which can be up to 11OO ° F (595 ° C) rich in the event that the Pyrolysereaktionszone is maintained at a temperature in the range of about 2OGO ⁰ F (1100 C) for a pyrolysis reaction , which is said to promote gasification, considerable amounts of carbon monoxide are formed.

Also, if the solids and combustion gases rise up through the riser 68, try to get into that Transport gas introduced carbon dioxide and the carbon dioxide formed by oxidation of the coal with additional Carbon in the coal react to form carbon monoxide according to the following reaction:

C + CO ₂ - > 2CO.

Therefore, it is generally less than half, and usually in the range of 20 to about 50%, of that Formation of the particle heating source in the transport gas, the required oxygen in the transport gas. The rest of the required Oxygen is introduced through the second burn zone to remove the carbon monoxide from the first burn zone To oxidize carbon dioxide.

Excess solids in the fluidized bed beyond requirement for oxidation to form the particulate heating source are the net solids product of the pyrolysis reaction and are evacuated through line 94 from the first chamber.

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The execution of the shown in the drawing and described above Firing unit has numerous advantages. Below this is the immediate ignition of the in the fluidized bed 60 incoming solids. The carbon contained in the carbonaceous solid residues becomes instantaneous oxidizes when exposed to a source of oxygen. When the carbonaceous solid residues have poor ignition properties Oxygen can be added with the fluidizing gas to remove the carbon in the solids to oxidize in the fluidized bed to raise the temperature of the fluidized bed. During the start-up, a Fuel gas can be used as fluidizing gas to keep the temperature of the solids in the fluidized bed above the ignition temperature of the solids.

Another advantage of the arrangement shown in the drawing and described above is that the temperature the first combustion chamber by controlling the proportion of oxygen supplied to the fluidized bed in the fluidizing gas flow 90 can be controlled.

Another advantage is the large amount of solids in the fluidized bed. Because of this large crowd will be minor system disturbances dampened by changing the level of the fluidized bed. When the level of the fluidized bed increases, additional solids are removed through vent 94 and additional solids through the Transport gas dragged along, as a higher pressure difference of the solids due to the growth of the fluidized bed level arises. But if, in the opposite case, the fluidized bed level falls, fewer solids become products drawn away and fewer solids are drawn in by the transport gases because the differential pressure of the flow

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bed falls off. If additional controls of the fluidized bed level are required, the flow rate of the oxygen source can be varied. Such is the fluidized bed is a self-compensating system.

Another advantage of the configuration of the first combustion chamber and the canister is because of the swirling of the Solids in the fluidized bed in the facilitation of the removal of the solid products. When the level of solids increases in the fluidized bed, more solids are automatically carried away through the solids outlet line 94. This conduit 94 extends upwardly in the container 52 and its height determines the average top edge of the fluidized bed in container 52.

A main advantage of the arrangement shown in the drawing is that a comparatively fail-safe Method for preventing oxygen from entering the combustion chamber 5O from the pyrolysis zone 8 is given. the The height of the fluidized bed 80 acts as a barrier to the reflux of oxygen through the tube 78 into the pyrolysis reactor. In addition, automatic control means can be provided which sense the level of the fluidized bed and, if the level drops too low, automatically cut off the flow of the oxygen source into the first combustion chamber .

The oxygen supply is through the gas inlet 82 into the second burning zone led. The amount of free oxygen introduced into the second burn zone is at least equal to 50 mole percent of the amount of carbon monoxide that completes the stage reached oxidized carbon monoxide, which is generated in the first combustion chamber, so that the entire

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possible calorific value of oxidized coal in the first combustion chamber is achieved. In addition, oxygen can above the stoichiometric amount can be added to react with the carbon in the coal to produce the Heat coal to the temperature required, the particle heating source for introduction into the pyrolysis zone to build. All of the oxygen supply to the two oxidation states is sufficient at all times to raise the solids to the temperatures required for the Feed to the pyrolysis zone is required. Typical particle heating sources are about 100 to 500 F (55 to 380 C) above the pyrolysis zone temperature. The induction of oxygen to oxidize the carbon Solid residues in two combustion chambers are used to achieve a maximum calorific value from the solid residues through oxidation obtain. When the solid residue is oxidized when a If there is less than the stoichiometric amount of oxygen and / or the residence time is long, try some of the carbon dioxide react to form carbon monoxide to create. This is undesirable because more valuable carbonaceous solids are burned must be in order to produce the desired temperatures, as if carbon dioxide are the only products. That eventually formed carbon monoxide is minimized and the ratio of carbon dioxide to carbon monoxide is increased maximized to the amount of free carbon generated per unit Maximize the amount of heat by burning the carbon using two combustion chambers.

The particle heating source formed and the gaseous combustion products of the solids, like non-reactive components of the oxygen source, such as nitrogen , go from the second combustion chamber to a second cyclone separator

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Ira separator 84 becomes the particle heating source from the fuel gases separated from the feed to the pyrolysis reaction zone. The gases 100 are passed through the top of the cyclone submitted. Since most of the carbon monoxide formed in the riser 68 and tube 54 is in the oxidation zone When oxidized to carbon dioxide, the combustion gases can be released directly into the atmosphere. if however, a significant amount of carbon monoxides or other contaminants in the combustion gas stream 100 from second cyclone separator 84 were present, these gases could be treated by chemical washing before they are released into the atmosphere.

Although the drawing shows the second combustion chamber zone and the second cyclone separator as separate devices shows, it is possible to form the particle heating source from the preheated solids and the particle heating source of the gaseous products of combustion at the same time in a common cyclone oxidation separation zone to separate.

There are significant benefits to this change. Among these benefits are reduced capital and operating costs for the process because the separator and combustor are replaced with a single cyclone separator. In addition, the production of carbon monoxide is minimized, since short reaction times, which favor the production of carbon dioxide, are obtained through the use of a cyclone container for the oxidation of the carbon-containing solid residue. Preferably, the residence times of the solids in the cyclone oxidation separation zone are less than 5 seconds and most preferably in the range of about 0.1 to about seconds. These short residence times favor the

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Production of carbon dioxide compared to carbon monoxide.

Another advantage of using a cyclone oxidation cleaning zone is that carbon-containing solid residue fines, which are valuable in their own right than larger particles, preferably because of more efficient separation the larger particles are burned by the fines in the cyclone.

The particle heating source obtained, separated from the gases in the second cyclone separation zone, passes through a pipe in the swirl chamber 32 surrounding the inlet to the pyrolysis reactor. The pipe 86 is traversed by a reference aeration gas that is not harmful to the pyrolysis products. The vent gas is introduced through inlets 88 inserted along the length of tube 86.

Although the invention has only been described with reference to a preferred exemplary embodiment, other embodiments are possible obvious to the person skilled in the art. For example, the carbon-containing solid residue can then enter the swirl chamber 3 injected to react with the hot particle heating source to generate hydrogen gas through water gas reactions to build. The hydrogen produced in this way can contain volatile hydrocarbons resulting from the pyrolysis of the carbonaceous Materials originate, hydrogenate to increase their value. In addition, one or more cyclones can be used if necessary can be used in series or in parallel to replace the cyclone separators 22, 84. The advantage of using of more than one cyclone in series is that a fines fraction of the carbonaceous solids residue and a fines fraction of the particle heating source from the cloud in the particle can be removed so that the amount of

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with the steam mixing to the effect of product recovery transferred solids is minimized.

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Claims (27)

BORIIMKRT & BOEHMLRT 0 158 claims 1. Process for the pyrolysis of solid carbonaceous material by heat transferred to this material from a particulate heating source, leaving a carbonaceous particulate matter residue obtained as a pyrolysis product and the particle heating source by oxidation of at least part of the solids-containing Solid particle residue is formed, characterized in that at least a part of the carbonaceous by pyrolysis Solid material formed carbonaceous Solid residue is brought to a fluidized bed surrounding a substantially vertically directed open tube, wherein the tube is in open communication with a substantially vertically directed riser and the tube and the riser pipe forming a first combustion chamber; that the solid residue from the fluidized bed into the first combustion chamber Injecting a gaseous source of oxygen up the tube to remove carbon in the solid matter partial heating of the solid residue to oxidize and around the solid residue and gaseous combustion products of the Solid residue, including carbon monoxide, a second To feed burning zone; and that a source of oxygen in the Second burning zone in a proportion of at least 50% of the molar feed of carbon monoxide is fed to the second burn zone so that all of the oxygen feed to the first and second 709881/0981 BOEIIMERT & BOKHMIlRT Burning zone is sufficient to generate the particle heating source. 2. The method according to claim 1, characterized in that the Line is at a distance from the riser pipe; and that the carbonaceous particulate residue in the fluidized bed by a Upward flow of a flowing gas is swirled into the riser through the space between the riser and the Line enters. 3. The method according to claim 1 or 2, characterized in that the fluidized bed by an oxygen-containing fluid gas is whirled. 4. The method according to any one of the preceding claims, characterized in that the carbonaceous solid material of a flash pyrolysis by continuous transport of the carbonaceous solid particulate material feed contained in the carrier gas, which is not deleteriously reactive with respect to the pyrolysis products, to a vertically directed, with Subjecting a downflow pyrolysis reactor, the pyrolysis reactor including a pyrolysis zone ^{operating at a temperature below about 2000 F (1100 0} C); in that the particle heating source is supplied to the pyrolysis reactor at a temperature above the pyrolysis temperature at a rate sufficient to maintain the pyrolysis zone at the pyrolysis temperature; that a turbulent mixture of the particle heating source, the carbonaceous particulate matter feed and the carrier gas is formed to pyrolyze the carbonaceous solid material feed and obtain a pyrolysis product stream which contains as solids the particle heating source and a carbonaceous solid pyrolysis residue and a vapor mixture of the carrier gas and the pyrolysis vapors - 709881/0981 BOEHMERT & BOEHMElRT Consist of hydrogen; and that the pyrolysis product stream from The pyrolysis reactor enters a first separation zone, so that at least the majority of the solids from the steam mixture is separated. 5. The method according to claim 4, characterized in that the first separation zone is a cyclone separation zone. 6. The method according to claim 4 or 5, characterized in that the particle heating source formed by the second combustion zone and the gaseous products of combustion are separated from one another in a cyclone separation zone. 7. The method according to any one of claims 4 to 6, characterized in that the second combustion zone is a cyclone oxidation separation zone forms. 8. The method according to claim 7, characterized in that the residence time in the cyclone oxidation separation zone below of about 5 seconds. 9. The method according to claim. 8, characterized in that the Residence time in e'er cyclone oxidation separation zone is below about 3 seconds. 10. The method according to any one of claims 4 to 9, characterized in that that the turbulent mixture in the pyrolysis reactor has a solids content in the range from about 0.1 to 10% by volume of the total Volume of stream possesses; and that the weight ratio of the particle heating source to the carbonaceous solid Material ranges from about 2 to 1 to about 20 to 1. 11. The method according to any one of claims 4 to 10, characterized 709881/0981 BOEHMERT & BOEHMIZR Γ draws that the pyrolysis zone is operated at a temperature above about 600 F (315 C). 12. The method according to claim 11, characterized in that the pyrolysis zone at a temperature in the range of 900 to 1400 ° F (480 to 770 ° C) is operated. 13. The method according to any one of claims 4 to 12, characterized in that the pyrolysis reactor has a solids inlet for the carbonaceous solid material feed and a has vertically directed chamber surrounding the upper part of the pyrolysis reactor, the inner peripheral wall of the Kanuner turned an overflow weir into a vertically directed mixing zone of the reactor forms; that the carbonaceous particulate matter is transported in a carrier gas to the solids supply inlet and is blown into the mixing zone there; that the particle heating source is directed to the vertically directed chamber and is related in the chamber by the flow of the essentially non-deleteriously reactive flowing gas is swirled onto the pyrolysis products; that the swirled particle heating source Discharged over the weir and down into the mixing zone to create a turbulent mixture with the carbonaceous To form particulate matter; and that the mixture passes down through the mixing zone to the pyrolysis zone of the pyrolysis reactor to remove the carbonaceous Pyrolize solid material. 14. The method according to any one of claims 4 to 13, characterized characterized in that the residence time of the carrier gas in the pyrolysis zone of the pyrolysis reactor and in the first Separation zone is below about 5 seconds. 15. The method according to claim 14, characterized in that 709881/0981 BOEHMERT & BOEHMEKT the residence time of the carrier gas in the pyrolysis zone of the Pyrolysis reactor and in the first separation zone is less than three seconds. 16. The method according to claim 15, characterized in that the pyrolysis time is in the range from 0.1 to 3 seconds. 17. The method according to any one of claims 4 to 16, characterized characterized in that a substantial proportion of the carbonaceous Materials are particles ranging up to about 1000 microns in diameter. 18. The method according to claim 17, characterized in that the carbonaceous material agglomerated carbon with a is substantially up to 250 micrometers in size. 19. Apparatus for forming a particulate heating source from a carbon-containing solid particle residue from pyrolysis of carbonaceous material to the pyrolysis of carbonaceous Solid material, characterized by a container (52) for receiving a fluidized bed (60) of the carbonaceous Solid particle residue of the pyrolysis around an open, essentially vertically directed tube (54); by a substantially vertically directed riser in open communication with the Riser pipe (68); Introducer means (22) for introducing the carbonaceous Particulate residue from pyrolysis into the fluidized bed (60); Injection means (56, 58) for injecting a gaseous Oxygen source up into the tube (54) for transfer of the carbonaceous residue from the fluidized bed into the Tube (54); and supply means (82) for supplying additional oxygen to the combustion chamber (70) to form the particle heating source. 709881/0981 BOEHMERT & ROCl IMERT 20. Apparatus according to claim 19, characterized in that that the tube (54) is separated from the vertical riser pipe (82). 21. Device for the pyrolysis of carbonaceous solids material characterized by a downflow pyrolysis reactor (10); by means (12, 24, 26) for training a turbulent mixture of the particle heating source and the carbonaceous solid material contained in a carrier gas for introduction into the pyrolysis reactor (1O) for pyrolysis of the carbonaceous solids feed are included to to form a pyrolysis product stream which is a vapor mixture and contains as solids the particle heating source and a carbonaceous solid residue from pyrolysis; through a first separator (22) for separating at least the majority of the solids from the vapor mixture in the pyrolysis product stream; by transfer means (18, 20) for transferring the pyrolysis product stream from the pyrolysis reactor (10) to the first separator (22); by means (52, 60) for forming the particle heating source, the consist of a container (52) which has a fluidized bed (60) of the separated solids around an open, essentially vertically directed tube (54), a substantially vertically directed riser tube (68) in open communication with the Tube (54), a combustion chamber (70) in connection with the riser pipe (68), supply means (56) for supplying a gaseous Oxygen source up into line (54) to Entrainment of the solids from the fluidized bed (6O) into the line (54) and means (82) for supplying oxygen to the combustion chamber (70) to heat the solids and form the particle heating source; by transmission means (78) for transmission the fuel solids from the first burner (22) to the fluidized bed (60); by means for transferring the particle heating source from the second combustor (70) to a second separator (84); 709881/0981 BOEHMERT & BOEHiMERT a second separator for separating the particulate heating source from the gaseous combustion product; and by means (86) for transferring the separated particle heating source from the second separator (84) to the pyrolysis reactor (10). 22. The device according to claim 21, characterized in that the tube (54) is separated from the riser pipe (68). 23. Device according to claim 21 or 22, characterized in that that the separator (22) is a cyclone separator. 24. Device according to one of claims 21 to 23, characterized in that the second separator (84) is a cyclone separator is. 25. Device according to one of claims 21 to 24, characterized in that the pyrolysis reactor (10) has a substantially vertically directed mixing zone (12) and a substantially vertically directed pyrolysis zone (14); that the Pyrolysis reactor (10), a solids supply inlet (24), a substantially vertically directed chamber surrounding the upper part of the reactor (10) and an inner peripheral wall (40) which forms an overflow weir (40) to the vertically directed mixing zone (12); and that the means (12, 24, 26) to form a turbulent mixture. Feed means (86) for feeding the particle heating source to a vertical one directional chamber (32); that supply means (42) for supplying the flowing gas into the chamber (32) is the particle heating source keep in a flowing state; and that injecting means (26) for injecting the im from the solids supply inlet (24) into the mixing zone (12) introduced carrier gas containing carbonaceous solids feed the resulting form turbulent mixture. 709881/0981 BOEHMERT & BC) FHMERT 26. Device for the pyrolysis of agglomerated coal, characterized by a pyrolysis reactor (10) with a downwardly directed Flow, the one substantially vertically directed mixing zone (12), one substantially vertically directed Pyrolysis zone (14), a solids feed inlet (24) and a has substantially vertically directed chamber (3 2) which surrounds the upper part (28) of the reactor (10), wherein the inner peripheral wall of the chamber (32) has an overflow weir (40) to the mixing zone (12), wherein the agglomerated coal feed contained in a carrier gas is connected to a particle heating source is connected under turbulent flow conditions in the pyrolysis zone (14) of the pyrolysis reactor (10) to a pyrolysis product stream to obtain, as solids, the particle heating source and a carbon-containing solid particle residue which contains pyrolysis as well as a steam mixture; by Supply means (86) for supplying the particle heating source to the vertically directed chamber (32); introducer (42) introducing a flowing gas into the chamber (32) to maintain the particle heating source in a flowing state therein; transfer means (26) for transferring the coal feed from the solids feed inlet (24) to the mixing zone (12); by a first cyclone separator (22) in connection with the pyrolysis reactor (10) for separating at least the main part of the Solids in the pyrolysis product stream from the steam mixture in the pyrolysis product stream; by means (52, 60) for forming the Particulate heating source consisting of a container (52) which holds a fluidized bed (60) of the separated solids around an open, substantially vertically directed tube (54), a substantially vertically directed riser tube (68) in open Connection with the vertically directed pipe (54) and separately a second combustion chamber (70) in connection with the Has riser pipe (68); by introducing means (56) for introducing a gaseous source of oxygen upwardly into the tube (54) for entrainment of the solids from the QE fluid bed (60) in BOEHMERT & BOEHMERT the tube (54) and to partially oxidize the carbon in the solids to remove the solids under additional Heat formation of combustion products; introducing means (82) for introducing oxygen into the second Combustor (70) for further heating the solids to form the particulate heating source; through a pipe (78) from first cyclone separator (22) to the fluidized bed (60) for transferring the separated solids from the first cyclone separator to the Fluidized bed (60); by a second cyclone separator (84) in communication with the combustion chamber (70) for separating the particle heating source from the gaseous products of combustion (110); and through a pipe (86) from the second cyclone separator (84) to the Chamber (32) containing the upper part (28) of the pyrolysis reactor (10) surrounds to transfer the particle heating source to the pyrolysis reactor (1O). 27. Device according to one of claims 19 to 26, characterized characterized in that the second combustion chamber and the second separator are integrated as a cyclone oxidation separator are trained. 709881/0981