DE102016210350A1 - Gasification reactor for the production of synthesis gases from solid gasification substances with the aid of oxygen-containing gasification agents - Google Patents

Abstract

The invention relates to a process and a gasification reactor for the production of synthesis gas from solid gasification substances by means of oxygen-containing gasification agent at elevated pressures using fluidized bed gasification (primary gasification), by means of a gasification reactor (v) with a gasification reaction space (v1) from bottom to top a post-oxidation fixed bed gasifier (a), a compound having a reaction space reaction, a primary gasification Wirbelschichtvergaser (b), a) wherein the reaction space of the primary gasification Wirbelschichtverggasers (b) directly or via a connector tube with the reaction space of Nachoxidations-fixed bed gasifier (a) is uninterrupted in communication and both form a common pressure space, the connection between primary gasification fluidized bed gasifier (b) and post-oxidation fixed bed gasifier (a) compared to the reaction spaces of primary gasification fluidized bed gasifier (b) and post-oxidation Festb In the post-oxidation reaction space (a2) in a post-oxidation moving bed, the reactor principle of the fixed-bed gasification, in the connection reaction space predominantly the reactor principle of entrained flow gasification and in the primary gasification reaction space (b1) the reactor principle of the central d) and the primary gasification of the introduced solid gasification substances with primary gasification agents (primary gasification-gasification agent) in the stationary fluidized bed, circulating fluidized bed, E) wherein the withdrawn from the primary gasification C-containing primary gasification bottom products nachoxidiert with post-oxidation gasification agents in the post-oxidation moving bed in countercurrent and part be gasified (post-oxidation).

Description

The invention relates to a process and a gasification reactor for the production of synthesis gases from solid gasification substances with the aid of oxygen-containing gasification agents.

The gasification of solid fuels in the fluidized bed has advantages compared to the flow gasification advantages in terms of lower oxygen consumption, lower gasification temperatures, lower raw gas temperatures, tolerance to higher ash contents or lower requirements for the fuel pretreatment (grain size 0 - about 5 mm). on. Particularly advantageous in this respect is the fluidized bed gasification for coals which have a high reactivity (brown coal, hard lignite, subbituminous coal, etc.). A modification of the classical fluidized bed gasification is the Spouted Bed Gasification, in which the gasification agents, consisting of oxygen, water vapor, CO ₂ or air alone or in mixtures, are injected at the bottom of the fluidized bed in high solids density areas, the solids around the gasifier jet / s solids circulate. In the areas where high temperatures occur due to oxidation, the released ash is sintered or melted and forms granules, which fall down to over a centimeter after reaching a certain size of several millimeters and are withdrawn as a bottoms product.

Two of the biggest drawbacks of why fluidized bed processes, such as the high temperature Winkler (HTW) process, have not been able to penetrate the market are the limited carburetor and crude gas temperatures and the lack of landfill capability of solid gasification residues. The expense for the gas treatment and for the aftertreatment of the gasification residues by gasification or post-oxidation is high. Overall, lower synthesis gas yields are offset by higher CO ₂ emissions.

The carburetor temperatures can not be freely selected. They are limited according to the ash melting behavior of the coal used upwards, to avoid that the ashes neither in the freeboard of the WS-carburetor nor during the cooling of the dust-laden raw gas cause disruptive deposits, caking or slagging. The particle temperatures at the gasifier outlet should be below a critical value, referred to below as the critical ash sintering limit. This is often very low in the coals used in fluidized bed gasifiers, which preferably have a high reactivity (lignite, hard lignite, subbituminous coal, etc.). Typical values for lignite are around 1,000 ° C, for "young" coal at around 1,100 ° C. When admixing biomass, the values decrease significantly. The temperature limitation has the consequence that the raw gas with increasing process pressures contains increasing amounts of undesired gas components and trace substances, such as, for example, aliphatic hydrocarbons from methane to C4 hydrocarbons or aromatic hydrocarbons BETX and naphthalene. The high methane contents up to 10% by volume and above virtually preclude the use of fluidized bed or bubble gasification at the high pressure level of up to 60 bar required for chemical syntheses.

In order to increase the temperatures of the fluidized bed gasification and to achieve complete gasification including post-oxidation of the solid gasification residues, various approaches are followed.

In DE 10 2007 006 982B4 the gasification should be carried out in a cylindrical fluidized bed reactor at temperatures up to the maximum ash melting temperature up to about 1200 ° C. In the freeboard above the fluidized bed but low-oxygen to-free gasification must be supplied to lower the temperatures of the gasifier leaving the dusty raw gases to values up to and below the kinetischen Reaktionsendtemperaturen, which are below the critical ash sintering limit. At low-carbon coals, the reaction end temperatures are at about 900 ° C and lower, so that due to equilibrium takes place a regression of methane, higher hydrocarbons or ammonia. The solution is therefore not suitable for achieving a fundamental improvement in gas quality. At the bottom of the fluidized bed, a moving bed follows, in which the post-gasification and post-oxidation of the carbon-containing gasification residues of the fluidized bed should take place. Apart from the fact that it is difficult because of local overburdening of the moving bed to form a uniform fluidized bed by randliche injection of gasification over the moving bed, required for the prevention of slagging rapid reduction of the temperature in the freeboard requires a high distribution overhead over the cross section. This is not easily ensured in fluidized-bed gasifiers of large lines.

DE 102007006980B4 follows a different approach. In Freeboard, a central hot spot is created, which is surrounded by a colder reaction space with endothermic reactions. Since the high temperatures occur in the top of the carburetor, large carburetor heights are required to ensure the necessary Abklinglängen for the high temperatures to the raw gas outlet. there also occur secondary reactions of new formation of methane, higher hydrocarbons or ammonia. Finally, the central hot spot does not cover the entire carburetor cross section, so that gases from the fluidized bed containing unwanted gas components flow up untreated to the crude gas outlet.

There are various approaches to treat the still strong carbonaceous, solid gasification residues (C> 5 wt .-%), which are the bottom products withdrawn below and the dust discharged with the raw gas. In particular, alternatives for the complex cooling of the hot, fine-grained to dust-like material for the production of the storage and transportability, and for the external afterburning, which is preferably carried out in a fluidized bed, are found. For the utilization of the dusts, it is advisable to trace them back to the gasifier as dry as possible, eg DE10 2007 006 981 B4 . DE 10 2007 006 982 B4 . EP 1 201 731 A1 ,

Proposed solutions for the post-gasification and post-oxidation of the bottom product in a moving bed strive for the simultaneous cooling of the post-oxidized soil products with the countercurrent, cold gasification agents. According to DE 10 2007 006 982 B4 under fluidized bed gasification, a moving bed for gasification of the bottom product at temperatures below the ash softening point is described. The practical implementation is greatly limited by the fact that the proposed formation of a uniform fluidized bed above the moving bed is difficult to achieve because the outflow over the cross section of the moving bed is not uniform, ie there are local landfills of non-coal or only partially gasified coal so that the gasification agents injected into these non-fluidized areas form slag. As a result, a uniform operation of the fluidized bed and in the wake of the moving bed is not guaranteed.

EP 1 201 731 A1 provides a second post-gasification zone in continuation of the narrowed cross section of the bottom product draw below the fluidized bed zone. In this zone are gradually injected gasification agent to liquid water. Since fluidization must be avoided, the supply of the gasification agents and the reaction conversion are severely limited. Complete post-oxidation of fluidised bed gasification products at higher C levels can not be ensured.

In DE 4 339 973 C1 The C-containing gasification residues of the fluidized bed gasification fed to an entrained flow gasifier and completely gasified in this. The high technical complexity is contrary to a realization, however.

In a modification of the fluidized bed gasification to an internally circulating fluidized bed gasification by using dusty coal suggests DE 10 2007 006 981 B4 to arrange a moving bed gasification below the internally circulating fluidized bed gasification with temperatures below the critical ash sintering limit. The ash granules formed in the internally circulating gasification are to fall down into the fixed bed where they are post-oxidized with oxygen-poor, secondary gasification agents. The dust discharged overhead is filtered out of the raw gas and completely returned to the gasifier. The proposal does not take into account that the gas from the fixed bed flows unevenly upwards across the cross section of the moving bed. The uneven gas flow and the accumulation and accumulation of non- or only partially gasified coal in the moving bed prevent the regular operation of this moving bed, so that the process in the proposed manner can be performed only limited.

DE 10 2013 107 311 A1 describes the arrangement of a Nachoxidationsreaktors below the fluidized bed, in which the sintering-free post-treatment of the C-containing bottoms product with oxidizing agents (O ₂ / steam or O ₂ / CO ₂ ) is provided. The supply of the oxidizing agent is provided with open-pored, ceramic elements, which can be arranged variable and varied over the height of the post-oxidation reactor. To control the process, the carbon content of the post-oxidized bottoms product should be measured continuously. Apart from the fact that the ceramic elements would need to be thermally shock resistant and exposed to extremely harsh conditions, complete post-oxidation would be difficult due to the uneven distribution of the oxidizer and C-containing bottoms across the height and cross section of the reactor.

The object of the invention is to develop a process and a gasification reactor for the production of synthesis gases from solid gasification substances with the aid of oxygen-containing gasification agents at high pressures, in which the carbon of the gasification substances is largely converted to form CO and subordinate to CO ₂ .

• a) wobei der Reaktionsraum des Primärvergasungs-Wirbelschichtvergasers (b) direkt oder über ein Konnektorrohr mit dem Reaktionsraum des Nachoxidations-Festbettvergasers (a) unterbrechungsfrei in Verbindung steht und beide einen gemeinsamen Druckraum bilden, wobei die Verbindung zwischen Primärvergasungs-Wirbelschichtvergaser (b) und Nachoxidations-Festbettvergasers (a) einen gegenüber den Reaktionsräumen von Primärvergasungs-Wirbelschichtvergaser (b) und Nachoxidations-Festbettvergasers (a) einen kleineren Querschnitt aufweist,
• b) wobei der Vergasungs-Reaktionsraum (v1) einen unterbrechungsfrei zusammenhängenden Reaktionsraum bildet, bei dem der Nachoxidations-Reaktionsraum (a2) mit dem Primärvergasungs-Reaktionsraum (b1) durch den Verbindungs-Reaktionsraum miteinander verbunden ist und der vom Ascheaustrag (a1) bis zum Rohgasabgang (b4) reicht,
• c) wobei im Nachoxidations-Reaktionsraum (a2) in einem Nachoxidations-Wanderbett das Reaktorprinzip der Festbettvergasung, im Verbindungs-Reaktionsraum überwiegend das Reaktorprinzip der Flugstromvergasung und im Primärvergasungs-Reaktionsraum (b1) das Reaktorprinzip der zentral-fluidisierten Sprudelschichtvergasung, übergehend in das der Strahlwirbelschichtvergasung, im Sekundärvergasungs-Reaktionsraum (b2) das Reaktorprinzip der Wirbelschichtvergasung angewendet werden,
• d) wobei die Primärvergasung der eingetragenen festen Vergasungsstoffe mit primären Vergasungsmitteln (Primärvergasungs-Vergasungsmittel) in der stationären Wirbelschicht, zirkulierenden Wirbelschicht, Strahlwirbelschicht oder Sprudelschicht durchgeführt wird,
• e) wobei die aus der Primärvergasung abgezogenen C-haltigen Primärvergasungs-Bodenprodukte mit Nachoxidations-Vergasungsmitteln im Nachoxidations-Wanderbett im Gegenstrom nachoxidiert und teilweise vergast werden (Nachoxidation),
• f) wobei die gebildeten Nachoxidations-Bodenprodukte (Aschen) als deponiefähige Aschen unterseits des Nachoxidations-Wanderbetts und die gebildeten Nachoxidations-Rohgase nach oben in die Primärvergasung abgezogen werden,
• g) wobei das Nachoxidations-Wanderbett im Nachoxidations-Festbettvergaser aus einem unteren zylindrischen Teil und einem oberen, sich einschnürenden Teil, dessen oberes Ende höchstens bis zum unteren Ende der Verbindung zum Primärvergasungs-Wirbelschichtvergaser (b) reicht, gebildet wird,
• h) wobei die aus dem Nachoxidations-Wanderbett nach oben steigenden Gase (umfassend Nachoxidations-Rohgase und weitere Gase) mit Strömungsgeschwindigkeiten in das untere Ende der Verbindung zum Primärvergasungs-Wirbelschichtvergaser (b) eingeleitet werden, die höchstens so groß sind, dass die das Nachoxidations-Wanderbett bildenden Primärvergasungs-Bodenprodukte, von oben aus dem Primärvergasungs-Wirbelschichtvergaser durch die Verbindung in das Nachoxidations-Wanderbett fallen können,
• i) wobei die aus dem oberen Ende der Verbindung nach oben in den Primärvergasungs-Wirbelschichtvergaser eintretenden Gase mit Strömungsgeschwindigkeiten eingeleitet werden, die mindestens so groß sind, dass die Primärvergasungs-Bodenprodukte oberhalb des oberen Endes der Verbindung fluidisiert werden,
• j) wobei die Menge der nach oben in das Nachoxidations-Wanderbett eingebrachten Nachoxidations-Vergasungsmittel und die Menge der aus dem Nachoxidations-Wanderbett nach unten abgezogenen Nachoxidations-Bodenprodukte so eingestellt werden, dass die Nachoxidation unterhalb des oberen Endes des zylindrischen Teils des Wanderbetts abgeschlossen ist,
• k) wobei in den Primärvergasungs-Reaktionsraum (b1) die festen C-haltigen Vergasungsstoffe über Vergasungsstoff-Einträge (b13) auf Höhen eingetragen werden, die zwischen dem oberen Bereich des sich konisch erweiternden Primärvergasungs-Reaktionsraums (b11) und dem unteren Bereich des zylindrischen Primärvergasungs-Reaktionsraums (b1) liegen,
• l) wobei die Primärvergasungs-Vergasungsmittel seitlich und/oder zentral mittels Vergasungsmitteldüsen (27) über die Primärvergasungs-Vergasungsmittel-Einträge (b14) auf Höhen eingetragen werden, die mindestens in der Zone der Zentralfluidisierung (b112) liegen und die bis zum unteren Bereich des zylindrischen Primärvergasungs-Reaktionsraums (b1) reichen,
• m) wobei die Primärvergasungs-Vergasungsmittel so eingedüst werden und die Vergasungsmittel-Düsenstrahlen mit Strömungsimpulsen versehen sind, dass sie die gegenüberliegenden Wände des Primärvergasers nicht berühren, und die Vergasungsmittel-Düsenstrahlen in die Zone der Zentralfluidisierung (b112) eindringen, sie jedoch nicht durchdringen, und in Verbindung mit den aus dem Nachoxidation-Wanderbett aufsteigenden Gasen zur Ausbildung einer Sprudelschichtvergasung ausgehend von der Zentralfluidisierung führen.

The object is achieved by a process for the production of synthesis, reduction and / or combustion gases from solid gasification substances with the aid of oxygen-containing gasification agents, the Water vapor and optionally CO2 as endothermic gasification agent containing, at elevated pressures using fluidized bed gasification (primary gasification), by means of a gasification reactor (v) with a gasification reaction chamber (v1), from bottom to top
a post-oxidation fixed-bed gasifier (a) having a pressure vessel with a post-oxidation reaction space (a2) for receiving a moving bed, with an ash discharge (a1) at the bottom of the post-oxidation fixed-bed gasifier (a), with a supply for post-oxidation gasification agent,
a connection to a connection reaction space,
a primary gasification fluidized bed gasifier (b) having a primary gasification reaction space (b1) with a zone for central fluidization (b112), with a multi-part primary gasification gasification agent entry (b14), with a plurality of gasification substance entries (b13), with a secondary gasification reaction space (b2) with a raw gas outlet (b4) at the top of the primary gasification fluidized-bed gasifier (b),
having,

• a) wherein the reaction space of the primary gasification Wirbelschichtverggasers (b) directly or via a connector tube with the reaction space of Nachoxidations-fixed bed gasifier (a) without interruption in combination and both form a common pressure chamber, the connection between primary gasification Wirbelschichtvergaser (b) and post-oxidation Fixed-bed gasifier (a) has a smaller cross section than the reaction spaces of primary gasification fluidized bed gasifier (b) and post-oxidation fixed bed gasifier (a),
• b) wherein the gasification reaction space (v1) forms an uninterrupted coherent reaction space in which the post-oxidation reaction space (a2) is connected to the primary gasification reaction space (b1) through the connection reaction space and from the ash discharge (a1) to the Raw gas discharge (b4) is sufficient
• c) wherein in the post-oxidation reaction space (a2) in a post-oxidation moving bed, the reactor principle of fixed bed gasification in the connection reaction space predominantly the reactor principle of entrained flow gasification and in the primary gasification reaction chamber (b1) the reactor principle of the central-fluidized bubbler gasification, passing into that of the fluidized bed gasification , in the secondary gasification reaction space (b2), the reactor principle of the fluidized bed gasification are used,
• d) wherein the primary gasification of the registered solid gasification substances is carried out with primary gasification agents (primary gasification-gasification agent) in the stationary fluidized bed, circulating fluidized bed, jet fluidized bed or effervescent layer,
• e) wherein the C-containing primary gasification bottoms withdrawn from the primary gasification are post-oxidized with post-oxidation gasification agents in the post-oxidation moving bed and partially gasified (post-oxidation),
• f) wherein the post-oxidation soil products (ashes) formed as depositable ashes under the post-oxidation moving bed and the formed post-oxidation raw gases are drawn off into the primary gasification,
• g) wherein the post-oxidation moving bed in the after-oxidation fixed-bed gasifier is formed of a lower cylindrical part and an upper constricting part whose upper end reaches at most the lower end of the connection to the primary gasification fluidized bed gasifier (b);
• h) wherein the gases rising from the post-oxidation moving bed (comprising post-oxidation raw gases and further gases) are introduced at flow rates into the lower end of the connection to the primary gasification fluidized bed gasifier (b) which are at most so large that the post-oxidation Moving bed forming primary gasification bottoms, can fall from above the primary gasification fluidized bed gasifier through the compound into the post-oxidation moving bed,
• i) wherein the gases entering the primary gasification fluidized bed gasifier from the upper end of the connection are introduced at flow rates at least sufficient to fluidize the primary gasification bottoms above the upper end of the connection,
• j) wherein the amount of post-oxidation gasification agent introduced upward into the post-oxidation moving bed and the amount of post-oxidation bottom products withdrawn from the post-oxidation moving bed are adjusted to complete post-oxidation below the upper end of the cylindrical part of the moving bed .
• k) wherein in the primary gasification reaction space (b1) the solid C-containing gasification substances via gasification substance entries (b13) are registered at altitudes between the upper region of the flared primary gasification reaction space (b11) and the lower portion of the cylindrical primary gasification reaction space (b1),
• l) wherein the primary gasification gasification agent is laterally and / or centrally by means of gasification agent nozzles ( 27 ) are introduced via the primary gasification-gasification agent entries (b14) to altitudes which are at least in the zone of central fluidization (b112) and which extend to the lower region of the cylindrical primary gasification reaction space (b1),
• m) wherein the primary gasification gasification agents are injected and the gasification agent jets are provided with flow pulses that do not contact the opposed walls of the primary gasifier and the gasification agent jets penetrate into, but do not penetrate, the zone of central fluidization (b112), and in conjunction with the gases ascending from the post-oxidation moving bed to form a bubble layer gasification from the central fluidization.

Advantageously, the oxygen content of the post-oxidation gasification agent is adjusted so that in the oxidation zone of the post-oxidation moving bed at most a permanent sintering and / or a local and temporally limited melting of the ash, but no slagging occurs.

According to one embodiment of the method according to the invention 70-95% of the oxygen of the total supplied gasification with the primary gasification gasification agents (primary gasification oxygen) and 30 - 5% with the post-oxidation gasification agents (post-oxidation oxygen) introduced.

According to a further advantageous embodiment of the method according to the invention is above the secondary gasification reaction space (b2) via quench nozzles ( 12 ) such quench water ( 22 ) that the temperatures of the secondary gasification raw gas laden with secondary gasification fine dusts are lowered to values below the critical ash sintering limits.

The invention also includes a gasification reactor for the production of synthesis, reduction and / or combustion gases from solid gasification substances with the aid of oxygen-containing gasification agents containing water vapor and optionally CO ₂ as endothermic gasification agent, at elevated pressures using fluidized bed gasification (primary gasification). .
with a post-oxidation fixed-bed gasifier (a) having a pressure vessel with a post-oxidation reaction space (a2) for receiving a moving bed, with a rotary grate with post-oxidation gasification feed means having an ash discharge (a1) at the bottom of the post-oxidation fixed bed gasifier (a),
with a primary gasification fluidized bed gasifier (b) having a primary gasification reaction space (b1) with a zone for central fluidization (b112), with a secondary gasification reaction space (b2), with a raw gas outlet (b4) at the top of the primary gasification fluidized bed gasifier (b) , with a multi-part primary gasification-gasification agent entry (b14), with several gasification substance entries (b13)
with a connection between post-oxidation fixed-bed gasifier (a) and primary gasification fluidized bed gasifier (b) as direct connection or connection via a connector tube for pressure-tight and uninterrupted connection of the reaction spaces of primary gasification fluidized bed gasifier (b) and post-oxidation fixed bed gasifier (a),
wherein the connection between primary gasification fluidized-bed gasifier (b) and post-oxidation fixed-bed gasifier (a) has a smaller cross section than the reaction spaces of primary gasification fluidized bed gasifier (b) and post-oxidation fixed bed gasifier (a),
wherein the gasification substance entries (b13) are arranged and configured as diagonal pipe entries on the primary gasification fluidized-bed gasifier (b) such that the gasification substances are introduced into the edge region of the primary gasification reaction space (b1),
wherein the multi-part primary gasification-gasification agent inlet (b14) comprises a plurality of circumferentially at least one level, at the lower end of the primary gasification fluidized bed gasifier equally distributed, downwardly sloping and on the primary gasification Vergaserachse in the zone of Zentralfluidisierung (b112) aligned primary gasification Vergasungsmittel- Nozzles ( 4 ) having,
wherein the primary gasification-gasification agent entry (b14) with the primary gasification-gasification agent nozzles (b14) 4 ) such that the primary gasification gasifying agents are injected and the primary gasifying agent jets are provided with flow pulses so as not to contact the opposed walls of the primary gasifier and the primary gasifying agent jets penetrate into the zone of central fluidization (b112), but they do not penetrate and, in conjunction with the gases ascending from the post-oxidation moving bed, lead to the formation of a bubbling gasification from the zone of central fluidization.

An embodiment of the gasification reactor according to the invention is that at the post-oxidation gas dome (a23) of the post-oxidation fixed-bed gasifier (a) additionally feeds ( 9 ) for post-oxidation process materials ( 35 ) are arranged.

When connecting the primary gasification fluidized-bed gasifier (b) and the post-oxidation fixed-bed gasifier (a) via the connector pipe (c), its upper end is flush in the bottom of the primary gasification fluidized-bed gasifier (b) and its lower end is flush or not flush in the post-oxidation gas dome ( a23 ) of the post-oxidation fixed bed gasifier (a),
wherein the contour of the connector tube (c) corresponds to a cylinder or a tube which widens toward the upper end and / or the lower end,
and wherein the length of the connector tube (c) is at least as large as its mean diameter.

According to a further advantageous embodiment of the gasification reactor according to the invention, the primary gasification fluidized-bed gasifier (b) has a quench zone reaction space (b3) above the secondary gasification reaction space (b2), in the quench nozzles ( 12 ) for the injection of quench water ( 22 ).

The reaction space of the primary gasification fluidized bed gasifier (b) is connected directly or via a connector pipe (c) to the reaction space of the post-oxidation fixed bed gasifier (a) without interruption. Both form a common pressure chamber, wherein the connection between the primary gasification fluidized bed gasifier (b) and post-oxidation fixed bed gasifier (a) has a smaller cross section than the reaction spaces of primary gasification fluidized bed gasifier (b) and post-oxidation fixed bed gasifier (a).

Direct connection means that the lower part of the bottom of the primary gasification fluidized bed gasifier (b) and the afteroxidation gas dome (a23) of the post-oxidation fixed bed gasifier (a) are connected so that the reaction space of the primary gasification fluidized bed gasifier (b) and post-oxidation gasifier Fixed bed gasifier (a) without interruption in connection.

A smaller cross-section of the compound means that the primary gasification bottoms forming the post-oxidation moving bed can fall from the top of the primary gasification fluidized bed gasifier through the compound into the post-oxidation moving bed.

The primary gasification of the registered solid gasification materials is carried out with primary gasification agents (primary gasification-gasification agent) in the fluidized bed or in the effervescent layer. Below the primary gasification, a post-oxidation gasification with a post-oxidation moving bed is arranged, in which the C-containing primary gasification bottoms withdrawn from the primary gasification are gassed countercurrently with post-oxidation gasifiers and post-oxidized (post-oxidation), the post-oxidation bottoms (ashes ) are withdrawn as landfillable ashes below the Nachoxidations-moving bed and the formed post-oxidation raw gases up into the primary gasification.

Above the primary gasification, a gas calming space, a raw gas outlet and one or more hot gas cyclones are arranged one after the other in the primary gasification for the separation and recycling of the dust gases containing C dust.

The hot gas cyclones leaving and loaded with C-containing fine dusts raw gases are subjected to a wet or dry total dedusting, (v) the deposited C-containing fines partially or completely returned to the primary gasification or partially or completely post-combusted in a furnace.

The gasification reactor (v) with a gasification reaction space (v1) comprises from bottom to top a post-oxidation fixed-bed gasifier (a) with an ash discharge (a1) at the bottom of the post-oxidation fixed-bed gasifier (a) and with a post-oxidation reaction space (a2), a direct connection or connection by means of a connector tube with a connection reaction space, a primary gasification fluidized bed gasifier (b) with a primary gasification reaction space (b1), with a secondary gasification reaction space (b2), if necessary with a quench zone reaction space (b3), and a raw gas outlet (b4) at the top of the primary gasification fluidized bed gasifier (b).

The gasification reaction space (v1) forms an uninterrupted coherent reaction space in which the post-oxidation reaction space (a2) is connected to the primary gasification reaction space (b1) through the connection reaction space and from the ash discharge (a1) to the raw gas outlet (b4 ) enough,
wherein in the post-oxidation reaction space (a2) in the post-oxidation moving bed, the reactor principle of fixed bed gasification, in the reaction space reaction chamber mainly the reactor principle of fluidized bed gasification and in the primary gasification reaction space (b1) the reactor principle of the central-fluidized bubbler gasification, passing into that of the fluidized bed gasification, in the secondary gasification -Reaktionsraum (b2) the reactor principle of fluidized bed gasification and in the case be provided if necessary quench zone reaction space (b3), the reactor principle of the fluidized bed gasification are applied in the reactor principle of entrained flow gasification.

The post-oxidation fixed-bed gasifier (a) comprises from bottom to top an ash discharge (a1), a post-oxidation reaction space (a2), a rotary grate (a21), a post-oxidation moving bed (a22), a post-oxidation gas dome (a23), at least one Post-oxidation process feed (a24) and a central top post-oxidation gas exit (a25).

The primary gasification reaction space (b1) has a bottom of the primary gasification reaction space (b11) that tapers conically upwards with a cone angle of 25-40, which merges into a cylindrical primary gasification reaction space (b12) and with at least one gasification substance inlet (b13), at least one primary gasification-gasification agent feed (b14) and if necessary, having at least one primary gasification process feed (b15).

The primary gasification reaction space (b11) is bounded at the bottom by a central bottoms removal (b111) of the primary gasification bottoms over which centrally extends a zone of central fluidization (b112), the secondary gasification reaction space (b2) being the primary gasification reaction space (b12) continues up to the quench zone reaction space (b3) or to the crude gas outlet (b4) at the head of the primary gasification fluidized-bed gasifier (b), if required.

The quench zone reaction space (b3), if necessary, continues the secondary gasification reaction space (b2) and has a lower quench area (b31) with at least one quench nozzle or at least one quench nozzle plane (b311) and an upper equalization area (b32) Crude gas outlet (b4) at the top of the primary gasification fluidized bed gasifier (b) ranges.

When connected to a connector tube (c) having a cylindrical or in diameter upwards steadily, conically slightly widening or downwardly steadily conical or stepped slightly widening connector tube reaction space (c1) and its ratio of length to medium, clear Diameter can be varied in the required for the apparatus engineering areas, which connects the central upper post-oxidation gas outlet (a25) with the central product withdrawal (b11) without interruption, and if necessary, a connector tube-process material entry includes.

According to an advantageous embodiment of the invention, the raw gas outlet is followed by direct or indirect cooling of the raw gases laden with fine dusts, separation of the fine dusts and provision of the cooled, separated wet or dry fine dusts. The fine dusts are separated from the water and recycled as primary gasification process materials into the primary gasification reaction space (b12).

When connected to a connector tube, the solid C-containing gasification substances are introduced into the primary gasification reaction space (b1) laterally via the gasification substance entries (b13), and laterally and / or centrally via the primary gasification-gasification agent entries (b14), the primary gasification-gasification agents. from top to bottom from the secondary gasification reaction chamber (b2) recirculating secondary gasification fine dusts, from bottom to top from the bottom product take-off (b111) the connector tube raw gases loaded with connector pipe dusts and, if necessary, laterally via the primary gasification process substance entries ( b15) primary gasification process substances introduced.

From the top of the primary gasification reaction space (b1), the primary gasification bottom products are discharged from top to bottom via the bottoms product discharge (b111) and from bottom to top from the cylindrical primary gasification reaction space (b12) the primary gasification crude gases loaded with primary gasification dusts.
the solid gasification materials being introduced at altitudes intermediate between the upper portion of the flared primary gasification reaction space (b11) and the lower portion of the cylindrical primary gasification reaction space (b12),
and wherein the primary gasification gasification agents are injected to altitudes at least in the zone of central fluidization (b112) and which may be up to the bottom of the cylindrical primary gasification reaction space (b12), and wherein the primary gasification process materials are directly at all altitudes the primary gasification reaction space (b1) or via the gasification substance entries (b13) can be entered.

In the secondary gasification reaction space (b2) are from bottom to top of the primary gasification reaction space (b12) loaded with primary gasification dust primary gasification crude gases and from top to bottom to be provided if necessary to be provided quench zone reaction space (b3) registered fine dusts and discharged from the secondary gasification reaction chamber (b2) from top to bottom recirculating secondary gasification fine dust and withdrawn from bottom to top loaded with secondary gasification fine dust secondary gasification crude gases, in the case of an unschanged quench zone reaction space (b3) from the bottom over represent the raw gas outlet (b4) withdrawn, loaded with fine dust raw gases.

In the quench zone reaction space (b3) to be provided if required, according to an advantageous embodiment of the method according to the invention via the quench region (b31) from bottom to top, the secondary gasification crude gases loaded with secondary gasification fine dust and from top to bottom, but also from bottom to top , or from the edge to the middle, but also from quench liquids, preferably quench waters, are injected into the middle of the edge via the quench nozzle levels (b311) and the quenched and quenched raw gases laden with fine dusts are withdrawn from the homogenization area (b32) of the quench zone reaction space (b3) from below laterally via the crude gas outlet (b4) and from top to bottom out of the quench zone reaction space (b3) quench zone fine dust discharged.

When connected to a connector tube, the primary gasification bottoms are injected into the connector tube reaction space (c1) from top to bottom via the central bottoms removal (b11) and from bottom to top through the central top post-oxidation gas exit (a25). Dust-laden post-oxidation raw gases registered and withdrawn from the connector tube reaction space (c1) from top to bottom, the connector tube bottom products and from bottom to top loaded with connector tube dusts raw connector tube crude gases. In the connector tube reaction space (c1) can be entered if necessary via a connector tube process material entry from top to bottom or from bottom to top connector process substances.

The post-oxidation reaction space (a2) is top-down through the central top post-oxidation gas outlet (a25) with primary gasification bottoms forming the post-oxidation moving bed (a22) with an upper limit post-oxidation heap cone and above postoxidation Gas dome (a23), and if necessary via a post-oxidation process material entry (a24) injected post-oxidation process materials in the post-oxidation gas dome (a23) and introduced via the rotary grate (a21) from bottom to top the post-oxidation gasification agent.

From the post-oxidation reaction chamber (a2), the afteroxidation crude gases laden with post-oxidation dusts are pumped from top to bottom via the central upper post-oxidation gas outlet (a23) and the cooled post-oxidation base products (C) from top to bottom via the ash outlet (a1) -free ash), deducted.

About the gasification substance entries (b13) dust-like to fine-grained, C-containing gasification materials with particle sizes corresponding to <about 0.5 mm to <about 2 mm and registered as required primary gasification process substances.

The amounts and compositions of the primary gasification gasification agents can be adjusted so that raw gas can be withdrawn from the raw gas outlet (b4) with the desired gas qualities and fine dusts, which are either completely gasified, i. have a landfillable, low carbon content, or whose carbon contents have deliberately higher values up to about 50 wt .-%.

The amounts and compositions of the post-oxidation gasification agents are adjusted to remove cooled, carbon-free, unmelted, sintered and at most partially melted ashes via the ash effluent (a1), the compositions of the post-oxidation gasification agents being adjusted so that it does not lead to dysfunctional slag formations in the post-oxidation reaction space (a2), and wherein the amounts of post-oxidation gasification agents are limited so that it does not come to non-regular, channel-like flows of the post-oxidation moving bed (a22).

According to an advantageous embodiment of the method according to the invention 70-95% of the oxygen of the total supplied gasification with the primary gasification gasification agents (primary gasification oxygen) and 30 - 5% with the post-oxidation gasification (post-oxidation oxygen) introduced.

The cross-section of the cylindrical part of the post-oxidation reaction space (a2) and the height of the post-oxidation moving bed (a22) measured from the upper edge of the rotary grate (a21) to the central upper post-oxidation gas outlet (a25) are according to an advantageous embodiment of the invention such that 60-90% of the ashes with P-content gasification grades with P-qualities are removed via the ash discharge (a1),

The empty tube velocities of the post-oxidation raw gases leaving the central bottoms removal (b111), based on the free cross section of the central bottoms removal (b111), advantageously have values well above the vortex point velocities, i. at speeds typical of fast fluidized beds to circulating fluidized beds, and are such that the zone of central fluidization (b112) extends at least to the level of the lowest primary gasification gasifier entries (b14) with their gasification agent jets in penetrate the zone of central fluidization (b112).

According to a further advantageous embodiment of the invention, the length of the cylindrical primary gasification reaction space (b12) is at least dimensioned so that the oxygen of the injected primary gasification gasification agent has chemically completely reacted before the primary gasification crude gases enter the secondary gasification reaction space (b2) ,

The cross-section of the cylindrical primary gasification reaction space (b12) and the secondary gasification reaction space (b2) are dimensioned according to an advantageous embodiment of the invention such that average flow velocities of secondary gasification withdrawn from the secondary gasification reaction space (b2) and loaded with secondary gasification particulate matter Set raw gases that correspond to those of the descent rates of the secondary gasification fine dust with specified discharge grain diameters in the range up to 0.1 mm.

Advantageously, the length of the secondary gasification reaction space (b2), including at least gasification pressure, gasification temperature at the upper end of the secondary gasification reaction space (b2) and reactivity of the secondary gasification fine dusts, so dimensioned that at least a sufficiently long time to set the values for the carbon contents of the quench zone fine dusts or fine dusts is set.

A quench zone reaction space (b3) is provided when the secondary gasification reaction space (b2) is to be limited to a level below the raw gas outlet (b4) to maintain the carbon-consuming endothermic gasification reactions at the desired carbon content values Freezing of secondary gasification fine dusts in the range up to approx. 50% by weight, and / or if the temperatures of the secondary gasification crude gases loaded with secondary gasification fine dusts are to be reduced to values below the critical ash sintering limits.

A lowering of the temperature in the quench zone reaction space (b3) to values below the critical ash sintering limits in the quench area (b31) is carried out in such a way that the quenching takes place by means of several quench nozzles in at least one quench nozzle plane (b311), which perform a quenching which is preferably close to the wall or uniform over the cross section to the extent that it has been concluded that at least one cooling of the quench zone fine dust close to the wall takes place at temperatures below the critical ash sintering limits at which it is not ensured to malfunctioning caking or deposits on the inner walls of the gasification reactor (v) up to and including the raw gas outlet (b4), and the subsequent homogenization range (b32) extends so far that the homogenization of the temperatures below the critical ash sintering limits is completed at least until the raw gas outlet (b4).

Advantageously, the primary gasification gasification agents are combusted by means of the primary gasification gasification agent entries (b14) comprising primary gasification gasification agent nozzles on at least one and at most three primary gasification gasification agent nozzle planes, each having at least three uniformly circumferentially distributed primary gasification gasification agents. Nozzles are included, whose gasification agent jets with angles of -30 ° to + 30 ° are directed against the horizontal and on the carburetor axis or at angles of <30 ° from the carburetor axis, injected. The gasification agent jets are provided with such flow pulses that they do not contact the opposing walls, and that the gasification agent jets of the at least bottom of the primary gasification / gasification agent nozzle planes penetrate, but do not penetrate, the zone of central fluidization (b112). The gasification agent jets of the top primary gasification-gasification agent nozzle plane do not extend substantially beyond the height, which marks the transition from the conical primary gasification reaction space (b11) into a cylindrical primary gasification reaction space (b12).

The primary gasification gasifiers may be in addition to or in lieu of the bottom of the primary gasification gasifier nozzle planes via a central primary gasification gasifier nozzle located on the gasifier axis at or above the central bottom product vent (b111) at the bottom of the zone of central fluidization (b112) is arranged to be injected vertically upwards.

The solid gasification substances are introduced laterally via the gasification substance entries (b13) gravimetrically by means of inclined tubes and / or mechanically by means of screw conveyors and / or pneumatically or hydraulically by means of pipelines, wherein one or more circumferentially distributed entries are provided and wherein the entries via the inclined tubes just above the height of the beginning of the conical primary gasification reaction space (b11).

By means of the process substance entries (a24), (b15) and the process substance entry of the connector tube (c), which consist of tubes or nozzles, can be gasified or thermally treated, gaseous, liquid or solid process materials or mixtures thereof into the reaction spaces (a2), (b1) or (c1) are introduced or injected, wherein gaseous and liquid process materials preferably in the reaction spaces (b1) and (c1) and solid process materials, such as the separated dry or wet fine dusts, preferably in the reaction space (a2 ) are introduced or injected.

The amounts of gaseous and / or gas injected into the post-oxidation gas dome (a23) Liquid process materials are adjusted so that the empty-tube velocities of the post-oxidation raw gases leaving the central bottoms removal (b111) are increased to the desired extent, whereby preferably the endothermically reacting gasification agents water vapor / evaporating water and / or CO2 are used.

Advantageously, almost the entire amount of the total supplied, endothermic gasification agent and steam possibly CO2 introduced with the post-oxidation gasification and the primary gasification gasification agents at least as much endothermic reacting gasifying admixed that a rinsing function is ensured at oxygen interruption.

In the manner according to the invention, the coupling of the five different fixed bed gasification, entrained flow gasification, fluidized bed gasification, fluidized bed gasification and fluidized bed gasification techniques into a new gasification reactor combines the principles in new ways, with advantages turn.

First, this involves coupling the fixed bed gasification to the bottoms removal (b111) of the centrally fluidized bubbler liquor bed gasification via a direct connection or connection by means of the connector tube (c).

The disadvantages of fixed-bed gasification, in this context the high excess of the endothermic gasification agent water vapor in the gasification agent and the low reaction conversion of the water vapor, raise the disadvantages of the bottom product takeoff of the fluidized-bed gasification, which in this context is the expensive bottom product cooling, the high C gas Content of the soil products and with increasing process pressure no longer reasonably realizable high gas supply or gas recirculation for the base fluidization, on. In the manner according to the invention, the coupling for the first time makes it possible to raise the process pressure of the bubble layer or fluidized-bed gasification to high process pressures> 60 bar without additional outlay for the base fluidization. The necessary according to the prior art feed or recirculation of large quantities of cold gases and their reheating omitted. The inferior, heated post-oxidation gasification gases with typical water vapor contents of 60 to 80% by volume are high quality gasification agents for gasification primary gasification fluidized bed gasifier (b). Advantageous use is made through the compound at the transition from the fixed bed to the central fluidized gasification stage of the connector tube (c) possible.

The central position of the direct connection or connection via the connector tube (c) eliminates a further disadvantage of the fixed-bed gasification, the lateral gas outlet, and thereby allows a symmetrical flow over the entire bed height of the post-oxidation moving bed (a22).

By coupling the fixed-bed gasification to the bottom product take-off (b111) by means of the connector tube (c) and the formation of a zone of intensive central fluidization (b112), which is surrounded by a bubble gasification, a new gasification principle of intensively mixed bubble gasification is created, here as central fluidized bubble gasification referred to. An important feature of the central fluidized bubbler gasification is the large distance of the opposed carburetor inner walls at the bottom, narrowest point of the bottoms removal (b111), at which the central fluidization begins. Accordingly, high volumes of primary gasification gasifiers may be injected laterally into the bottom product off-take (b111) by means of the primary gasification gasifier entries (b14) with only a few primary gasification gasification nozzles at a small vertical distance, without touching the opposing walls. The already strong central fluidization (b112) at the bottom of the gasification reactor is further enhanced by the gasification agent jets which penetrate into the zone of central fluidization (b112).

The primary gasification reaction space (b11) can therefore be equipped with a much stronger cone angle of the primary reaction space of 25-40 ° compared to the classical fluidized bed gasification of <25 °. The upwardly directed central fluidization (b112) can advantageously be achieved with a vertical upward injection of primary gasification gasification agent via a central primary gasification gasification agent nozzle located on the gasifier axis at or above the central bottom product vent (b111) in the lower Area of the zone of central fluidization (b112) can be combined. With this central primary gasification gasification agent nozzle, theoretically the entire primary gasification gasification agent can be introduced, whereby a far upwardly extending, central gasification agent jet is formed, which lengthens the height of the primary gasification reaction space (b1).

To reduce the height of the gasification reactor, it is therefore advantageous if, in addition to or instead of the mono-injection via the central primary gasification-gasification agent nozzle, the lateral injection of primary gasification Vergasungsmitteln via at least one primary gasification-gasification agent nozzle level takes place. The concentrated, lateral injection is particularly advantageous because the strong, near-ground fluidization with their high heat and mass transfer highest energy densities for the highly exothermic chemical reactions of the oxygen by partial oxidation allows, whereby the gasification agent jets of the top primary gasification gasification agent nozzle level a height can be limited that marks the transition from the conical primary gasification reaction space (b11) into the cylindrical primary gasification reaction space (b12).

Adjusted to the material and process conditions at which the gasification is to be carried out, one to three primary gasification agent gasifier nozzle levels are to be used, with one primary gasification gasifier nozzle having at least three uniformly circumferentially distributed primary gasification gasification agent nozzles for symmetry reasons Gasification agent jets are directed at angles of -30 ° to + 30 ° to the horizontal and to the carburetor axis or at angles of <30 ° to the carburetor axis. Preference is given to using primary gasification / gasification agent nozzles directed downwards of 10-20 ° and oriented centrally on the gasifier axis. Gasifier jet jets directed away from the carburetor axis are used to better utilize the primary gasification reaction space (b11) by an impinged swirl flow, preferably at the higher primary gasification / gasification agent nozzle levels.

Centrally fluidized bubbler gasification eliminates a significant disadvantage of prior fluidized bed or bubbler gasification, which is the need for severe constriction of the cylindrical gasifier space to a narrow bottom product take-off. In the classical fluidized bed this is realized by an elongated, conically narrowing reaction space, which causes an unnecessary extension of the reaction space of the fluidized bed gasifier and must be fluidized by means of many stepped over the height of the gasification agent nozzle levels. In the prior art bubbler gasification, high fluidization overhead is required across the entire (sieve) bottom of the bubbler gasifier.

Second, the previously insurmountable limitations of the gasification temperatures of the fluidized bed or bubble layer gasification and the entrained flow gasification are repealed. The previous fluidized bed or the bubbling gasification works at low temperatures below the ash melting point, which is why, despite the use of a recycle cyclone no complete C conversions can be achieved and the raw gases contain high levels of unwanted gas components and trace substances. In contrast, full C conversions and high quality raw gases are achieved in the entrained flow gasification, but at the available short residence times in the carburetor only using high carburetor temperatures above the ash flow temperatures. The disadvantages of the separately operated reactor principles are overcome by the combination and superposition of the reactor principles in connection with the use of the solid gasification materials in a specific grain size ranging from 0-0.1 mm to about 0-2 mm.

The superimposition of fixed bed gasification, entrained flow gasification, centrally fluidized gasification and fluidized bed gasification reactor regimes allows the gasification temperatures to be shifted to atypically high values for fluid bed and bubble bed gasification and atypically low for entrainment gasification. For example, for lignite for the first time, the gasification temperatures at the top of the secondary gasification reaction space (b2) can be raised to 1100 ° C and above, closer to the melting point of e.g. 1,250 ° C are brought here, wherein prevail in the gasification agent gases locally gasification temperatures well above the pour point of about 1400 ° C. The use of very high temperatures in the centrally fluidized bubbling gasification in the primary gasification reaction space (b1) and untypical high temperatures in the fluidized bed gasification in the secondary gasification reaction space (b2) allows the application of high pressures up to 60 bar and above, which for the first time required for synthesis gas gas qualities, For example, low methane levels less than 5 vol .-% at a pressure of 60 bar and above, can be achieved. With the increase in pressure, a reduction in the gas velocities, i. E. an increase in the residence time, as well as an increase in the partial pressures of the endothermic gasification agent reacting steam and carbon dioxide. Thus, the reaction rate of the endothermic gasification processes increases, so that only small residence times in the secondary gasification reaction space (b2) of a few seconds are sufficient for the complete or the desired carbon conversion.

The specific grain size of the solid gasification materials in the range 0-0.1 mm to approx. 0-2 mm, which lies between the values typical for fly-by-gas gasification and those for fluidised bed gasification of <0.1 mm and <4-6 mm, On the one hand, it is ideal for centrally fluidized gasification of the bubbling gas and, on the other hand, for the final gasification under the conditions of Fluidized bed gasification in the secondary gasification reaction space (b2). In the centrally fluidized liquefied-bed gasification, particle sizes above the dust grain size> 0.1 mm are required in order to avoid excessive discharge from the primary gasification reaction space (b11), on the other hand the typical values for fluidized-bed gasification <4-6 mm would be too coarse to in the desired high, related to the cross-section carburetor in a few seconds to reach the full to desired carbon conversions of secondary gasification fine dust with carbon contents in the range up to about 50 wt .-%. This is only possible if the secondary gasification fine dusts entering the secondary gasification reaction space (b2) have a grain size which is only so great that the secondary gasification fine dusts or fine dusts withdrawn from the secondary gasification reaction space (b2) have a particle diameter in the range up to 0 , 1 mm.

In the following, the reactor principles in the various reaction spaces on the way of the solids, first down to the ash outlet (a1) and then up to the crude gas outlet (b4) will be briefly explained. The solid gasification substances and possibly the primary gasification process substances are introduced via the gasification substance entries (b13) close to the wall into the conically widening primary gasification reaction space (b11). They are registered at heights between the upper part of the flared primary gasification reaction space (b11) and the lower part of the cylindrical primary gasification reaction space (b12). As gasification substance entries (b13) are inclined tubes for gravity input and / or screw conveyor for the mechanical entry and / or piping for the pneumatic or hydraulic entry in question, the height of the entry through the inclined tubes just above the height of the beginning of the conical primary gasification Reaction space (b11) is located.

The solid gasification materials are transported by the near-wall downflow by gravity predominantly into the zone of central fluidization (b112). From here, most of the solids are transported upwards and react at locally very high temperatures up to> 2,000 ° C with the side and / or centrally injected primary gasification gasification agents. The grain sizes of the carbonaceous gasification substances are reduced and the liberated ash melts and agglomerates to form melt agglomerates. Throughout the primary gasification reaction space (b11), there are so intense heat and mass transfer conditions that the incoming solid gasification substances and possibly the primary gasification process substances are mixed and heated on the shortest route and the gasification materials and molten ashes or melt agglomerates heated by the oxidation reactions cool down as quickly and freeze. The extreme fluidization in the zone of central fluidization (b112) is due to high flow rates of the raw gases flowing up from the bottoms removal (b111) which are well above the vortex point velocities, i. at typical for fast fluidized beds to circulating fluidized beds speeds are reached. It is assisted by the injection of the primary gasification gasification agent directed towards the zone of central fluidization (b112) and extends it upwards. The height of the zone of central fluidization (b112) reaches - without this extension - at least double to five times the diameter of the bottom product take-off (b111). Although the highest energy densities occur in the primary gasification reaction space (b11) as a result of the highly dominant, exothermic reactions of the partial oxidation, the high carbon concentrations of the circulating solids permanently ensure that the gasifier walls remain free from ashes or slag caking or slagging in the Flows of the bubble layer gasification occur. The circulation flow of the central fluidized bubbling gasification around the zone of central fluidization (b112) is so strong that a strong conical expansion of the bottom of the primary gasification reaction space (b11) to the cylindrical primary gasification reaction space (b12) with cone angles of 25-40 ° is possible without having to fluidize the floor with additional gas feeds.

Some of the solids, that is, the primary gasification bottoms, sink countercurrent to the raw gases that flow up and exert a sifter through the central bottoms removal (b111) into the union tube reaction space (c1). The primary gasification bottoms consist mainly of coarser and heavier, ash-rich particles including the resulting ash agglomerates, with grain sizes ranging up to 10 mm. Since the temperatures of the primary gasification bottoms are usually much higher than those of the countercurrent secondary gasification crude gases, endothermic gasification reactions take place in the connector reaction space as the primary gasification bottom products cool down, ie the carbon contents of the downwardly leaking connector well bottom products are somewhat lower than that the primary gasification bottom products entering from above. The flow conditions in the connector tube reaction space (c1) can change or overlap between a channel-like moving bed flow and a pneumatic conveying, the reactor principle of Fugitive gasification dominates. Especially in the vicinity of the central upper post-oxidation gas outlet (a25), a further particle size and density separation takes place in favor of coarser and heavier ash-rich particles as feedstock for the post-oxidation moving bed (a22).

The geometric configuration of the connector tube reaction space (c1) can be adapted to the requirements of the concrete application of the gasification reactor (v) in terms of length, diameter, diameter extensions, inlet and outlet design in a variety of ways, e.g. the ratio of length to average diameter according to an optimal apparatus engineering execution. Advantageously, the constricted pressure jacket of the primary gasification Wirbelschichtvergaser (b) with the likewise constricted pressure jacket of the post-oxidation fixed-bed gasifier (a) by a flange in the amount of the connector tube (c) be interconnected. It is also possible to install an adjustable slide valve in the flange connection, with which the two reaction chambers can be separated from one another on the solids side, if necessary (for example, for starting or stopping the gasification reactor (v)).

The connector tube bottoms exiting downward from the post-oxidation gas exit (a25) pass into the post-oxidation moving bed (a22) to form the post-oxidation bulk cone and the post-oxidation gas dome (a23). In the post-oxidation reaction space (a2), the reactor principle of the fixed-bed gasification is realized, which in contrast to the usual Lurgi fixed bed gasification of coals according to the prior art in Nachoxidations moving bed (a22) no drying and pyrolysis zone is present and bed is present, the essential hotter and in most cases much finer. According to the material and granulometric properties of the post-oxidation moving bed (a22), the compositions and the amounts of post-oxidation gasification agents are adjusted. As far as the compositions are concerned, the preferred control quantity is the so-called steam / oxygen ratio, expressed in kg of steam per Nm ^{3 of} oxygen. This is adjusted so that by means of the rotary grate (a21) unmelted, sintered and at most partially melted ashes are removed and it does not lead to disruptive slag formations in the post-oxidation reaction space (a2). Typical values for the steam / oxygen ratio are 5-7 kg / Nm ³ for gasifiers with high ash melting points and 7-10 kg / Nm ³ for those with low ash melting points. As for the amounts of post-oxidation gasification agents, the preferred control quantity is the real oxygen level or the area specific oxygen load. The surface-related amount of oxygen is limited according to the grain sizes of the ashes forming in the post-oxidation moving bed (a22) so that non-regular, channel-like flows through the post-oxidation moving bed (a22) do not occur. Typical values are from 200 to 500 Nm ³ Saueroffoff / m ² cross-sectional area of the Nachoxidations-Wanderbetts (a22) depending on the granularity of the beds.

The post-oxidized, dumpable ashes with carbon contents <5% by mass are discharged by means of the rotary grate (a21) into the ash discharge (a1), the rotating grate (a21) corresponding to the temperatures of the discharged, cooled ashes lying in a corridor of 100-200 K above the temperatures of the post-oxidation gasification agent is controlled.

The centrally fluidized bubbling gasification in the primary gasification reaction space (b1) extends over the conical primary gasification reaction space (b11) into the cylindrical primary gasification reaction space (b12). Here, the hot gas-solid jet and the large-scale solid recirculation flow of a jet fluidized bed in a fluidized bed, in which the flow velocities and the temperatures of the loaded primary gasification dust primary gasification crude gases over the cross-section and prevails the reactor principle of a fluidized bed gasification , In the primary gasification reaction space (b12) enter from the secondary secondary gasification reaction chamber (b2) recirculating secondary gasification fine dust.

The hot primary gasification raw gases withdrawn from bottom to top into the secondary gasification reaction space (b2) loaded with carbon-rich primary gasification dusts are the result of the predominantly occurring reactions of total oxidation to form CO ₂ and H ₂ O. They cool the secondary gasification reaction space (b2) as a result of the endothermic, carbon-consuming gasification reactions to form CO and H ₂ . The gasification temperatures characteristic of the gasification are the settling temperatures of the endothermic gasification reactions which occur at the upper end of the secondary gasification reaction space (b2). The grain sizes of the primary gasification dusts are reduced to the discharge grain diameter of the secondary gasification fine dust, which are withdrawn with the secondary gasification raw gas from the secondary gasification reaction space (b2), wherein the carbon contents decrease. In order to achieve the given, low discharge particle diameter of the secondary gasification fine dusts with values smaller than 0.1 mm, the mean flow velocities of the secondary gasification reaction space (b2) withdrawn, loaded with secondary gasification fine dust secondary gasification crude gases set correspondingly low. The achievable in connection with high gasification pressures, low flow velocities of secondary gasification crude gas laden with secondary gasification fine dust are an important feature of the invention. They allow the largely complete to desired carbon sales over a short path length of the flow, ie at low height of the gasification reactor (v). In the secondary gasification reaction space (b2), particle sizes decrease from bottom to top. The reactor principle prevails in fluidized bed gasification. This range is extended so long that secondary gasification fine dusts or fine dusts are withdrawn from the bottom to the top into the quench zone reaction space or into the raw gas outlet, which are either completely gasified, ie have a low carbon content capable of landfilling, or their carbon contents are deliberately higher to about 50% by mass. In the case of gasification at high temperatures, where the temperatures are adapted to the reaction capabilities of the solid gasification materials, and favored by high gasification pressures, complete gasification of the dusts is completed in only a few seconds. Predetermined, higher values for the carbon contents up to about 50% by weight are achieved by a correspondingly shorter secondary gasification reaction space (b2) or lower gasification temperatures at the upper end of the secondary gasification reaction space (b2). High carbon contents are desirable, for example, at high gasification temperatures as a so-called plaster carbon in order to avoid slagging or laying. In the case of gasification at low temperatures at the end of the secondary gasification reaction space (b2), for example, to produce methane-rich raw gases, high carbon contents of the secondary gasification fine dust are also sought.

In the case of gasification at high temperatures at the end of the secondary gasification reaction space (b2), it may be advantageous or necessary if above the secondary gasification reaction space (b2) a quench zone reaction space (b3) is arranged whose function is in the quench area (b31) quenching liquids, preferably quench water, inject. The amount of quenching liquids to be injected is adjusted so that the temperatures above the quench zone reaction space (b3) are lowered to values below the critical ash sintering limits. The injection takes place by means of several quench nozzles in at least one Quenchdüsenebene (b311) either cross-sectionally equal or at least close to the wall. The homogenization area (b32) which adjoins the quench area (b31) is expanded so far that the homogenization of the temperatures below the critical ash sintering limits is completed at least until the crude gas outlet (b4). The injected quench water not only cools the quench zone fine dust. In the quench zone reaction space (b3), under the prevailing conditions of fluidized bed gasification, the quench waters also transition into entrainment gasification to some extent with the carbon of the carbonaceous quench zone particulate matter, forming carbon monoxide, carbon dioxide and hydrogen. From the homogenization zone (b32), the quenched and cooled raw gases laden with fine dusts are drawn off above the crude gas outlet (b4) at the top of the primary gasification fluidized-bed gasifier (b). The quenching process can be used to advantage for pollutant disposal. As quenching liquids come next to be treated thermally treated wastewater, which are contaminated with inorganic or organic substances, and chemically treated liquids, such as ammonia waters in question.

The gasification reactor (v) is dimensioned and designed according to the given boundary conditions. The most important boundary conditions are the thermal performance, the raw gas quality, the properties of the solid gasification substances and the gasification pressure. The main criteria for the dimensioning of the main dimensions height and diameter of the primary gasification reaction space (b1) and the secondary gasification reaction space (b2) are the required residence times of the solid gasification materials, so that the vast majority gasification of the gasification materials used is guaranteed, which is expressed therein in that 70-95% of the oxygen of the total supplied gasification agent is introduced into the primary gasification reaction space (b1) with the primary gasification gasification means (primary gasification oxygen). The low values are for less reactive coals, especially hard coal, where the proportion of post-oxidation is higher, and the high values for reactive coals, such as lignite. The post-oxidation reaction space (a2) is dimensioned with respect to the cross section of the cylindrical part and the height of the post-oxidation moving bed (a22) measured from the upper edge of the rotary grate (a21) to the central upper post-oxidation gas outlet (a25) -90% of the ashes introduced with the solid C-containing gasification substances can be withdrawn via the ash outlet (a1). For this purpose, 30 to 5% of the total oxygen supplied with the post-oxidation gasification agents (post-oxidation oxygen) is to be introduced via the rotary grate (a21).

On the basis of in 1 The schematic diagram of a gasification reactor shown for generating synthesis gas from solid gasification substances with the aid of oxygen-containing gasification agent, the invention is described in more detail.

The gasification reactor (v) with a gasification reaction chamber (v1) is from a post-oxidation fixed-bed gasifier (a) with a pressure vessel with a Nachoxidations reaction space (a2) for receiving a moving bed, with a ash discharge (a1) at the bottom of Nachoxidations-fixed bed gasifier (a ), with a rotary grate (a21) with feed for post-oxidation gasification agent ( 36 ), a connector pipe (c) having a connector pipe reaction space (c1), a primary gasification fluidized bed gasifier (b) having a primary gasification reaction space (b1) having a central fluidization zone (b112), a secondary gasification reaction space (b2), with a quench zone reaction space (b3) with quench nozzles ( 12 ) for the injection of quench water ( 22 ), with a raw gas outlet (b4) at the top of the primary gasification fluidized bed gasifier (b), with a multi-part primary gasification gasification agent entry (b14), with a plurality of gasification substance entries (b13).

The gasification reaction space (v1) is a reaction chamber without interruption, in which the post-oxidation reaction space (a2) is connected to the primary gasification reaction space (b1) via the connector pipe reaction space (c1) and from the ash discharge (a1) to to the raw gas outlet (b4) ranges.

The post-oxidation fixed-bed gasifier (a) comprises an ash discharge (a1) and a post-oxidation reaction space (a2) comprising a rotary grate (a21), a post-oxidation moving bed (a22), a post-oxidation gas dome (a23 ), a post-oxidation process material feed (a24) in the form of a post-oxidation-process nozzle level ( 8th ) of 6 circumferentially-spaced post-oxidation process jets ( 9 ) and a central top post-oxidation gas outlet (a25).

The primary gasification reaction space (b1) is viewed from a bottom, which, as seen from the bottom upwards, extends conically upwards with a cone angle of 45 ° ( 2 ) of the conical primary gasification reaction space (b11) equipped with a multi-part primary gasification-gasification agent inlet (b14), which merges into a cylindrical primary gasification reaction space (b12) equipped with three gasification substance entries (b13) and primary gasification process substance entries (b15).

The multi-part primary gasification-gasification agent inlet (b14) consists of two superimposed primary gasification-gasification agent nozzle planes ( 3 ) with six circumferentially equally distributed primary gasification / gasification agent nozzles ( 4 ). The primary gasification-gasification agent nozzles ( 4 ) are arranged offset one above the other, with a tilt angle ( 5 ) Tilted 15 ° downwards and centered on the carburetor axis. The lower primary gasification-gasification agent nozzle level ( 6 ) is at the level of the first third of the conical bottom ( 2 ) and the upper primary gasification-gasification agent nozzle level ( 7 ) at the level of 90% of the conical bottom ( 2 ) arranged. The primary gasification gasification nozzles are water-cooled and wear-protected mixture nozzles, with which oxygen and steam are injected in the mixture.

The lower end of the conical primary gasification reaction space (b11) forms the central bottoms removal (b111) over which the C-containing primary gasification bottoms (b111) 30 ) are withdrawn into the connector tube (c).

The secondary gasification reaction space (b2) represents the connection of the cylindrical primary gasification reaction space (b12) with the quench zone reaction space (b3). This consists of a lower quench area (b31) with a quench nozzle plane (b311) and an upper homogenization area (b32) which up to the raw gas outlet (b4) at the head ( 1 ) of the primary gasification fluidized bed gasifier (b).

The connector tube (c) comprises a cylindrical connector tube reaction space (c1) whose length to diameter ratio 4 is.

The following describes the substances entering and leaving the reaction chambers. For a better understanding of the functioning are in 1 the fluids are shown with dashed arrows and the solids with solid arrows.

In the primary gasification reaction space (b1) are via the gasification substance entries (b13) by means of diagonal pipe entry the solid C-containing gasification materials ( 25 ), via the primary gasification-gasification agent entries (b14), the primary gasification-gasification agents ( 27 ), from top to bottom from the secondary gasification reaction space (b2) recirculating secondary gasification fine dusts ( 40 ), from bottom to top, from the bottom product extractor (b111) with the connector tube dusts ( 32 ) laden raw-tube connectors ( 33 ) and the primary gasification process inputs (b15) primary gasification process 26 ) brought in.

From the top of the primary gasification reaction space (b1), from top to bottom, via the bottoms product vent (b111), the primary gasification bottoms ( 30 ) and from bottom to top of the cylindrical primary gasification reaction space (b12) with the primary gasification dusts ( 28 ) loaded primary gasification crude gases ( 29 ).

The solid gasification substances ( 25 ) are introduced at heights between the upper portion of the flared primary gasification reaction space (b11) and the lower portion of the cylindrical primary gasification reaction space (b12). The primary gasification-gasification agents ( 27 ) of the lower primary gasification / gasification agent nozzle level ( 6 ) are injected at a height that the primary gasification gasification agent ( 27 ) enter the zone of central fluidization (b112) and expand it upwards.

The primary gasification process substances (B15) registered via the primary gasification process inputs ( 26 ) also include those from fine dust ( 20 ) loaded raw gas ( 21 ) in a water wash separated, wet fine dust.

In the secondary gasification reaction space (b2) are from bottom to top of the primary gasification reaction space (b1) with the primary gasification dusts ( 28 ) loaded primary gasification crude gases ( 29 ) and from top to bottom from the quench zone reaction space (b3) recirculating quench zone fine dust ( 42 ).

From the secondary gasification reaction space (b2) are from top to bottom secondary gasification fine dust ( 40 ) and from bottom to top the secondary gasification fine dusts ( 23 ) laden secondary gasification crude gases ( 24 ) deducted.

In the quench zone reaction space (b3), the bottom quench zone (b31) is filled with secondary gasification fine dust (from bottom to top). 23 ) laden secondary gasification crude gases ( 24 ) and are via quench nozzles ( 12 ) in the quenching nozzle levels (b311) quench water ( 22 ) injected. From the homogenization zone (b32) of the quench zone reaction chamber (b3), the particles with fine dusts ( 20 ) loaded, quenched and cooled raw gases ( 21 ) and from top to bottom out of the quench zone reaction space (b3) quench zone fine dusts ( 42 ).

After leaving the raw gas (b4), an in 1 untreated crude gas water washing with fine dusts ( 20 ), whose C content amounts to approx. 50% by weight, loaded raw gases ( 21 ) by means of a venturi scrubber. The fine dusts ( 20 ) are separated from the water and used as primary gasification process materials ( 26 ) are recycled to the primary gasification reaction space (b12).

Into the connector tube reaction space (c1) from top to bottom via the central bottoms removal (b11) are the primary gasification bottoms ( 30 ) and from bottom to top, via the central top post-oxidation gas outlet (a25), with post-oxidation dusts ( 37 ) laden post-oxidation raw gases ( 38 ).

From the connector tube reaction space (c1) are from top to bottom the connector tube bottom products ( 34 ) and from bottom to top with the connector tube dusts ( 32 ) laden raw-tube connectors ( 33 ) deducted.

In the post-oxidation reaction space (a2), from above to below via the central upper post-oxidation gas outlet (a25), the connector tube soil products ( 34 forming the post-oxidation moving bed (a22) with an upper limit in the form of a post-oxidation bulk cone ( 11 and above a post-oxidation gas dome (a23) and via the post-oxidation process feed (a24) by means of post-oxidation process gas nozzles (a23). 9 ) Post-oxidation process materials ( 35 ), which comprise concentrated wastewaters from the crude gas water scrubbing, are injected into the post-oxidation gas dome (a23) and, via the rotary grate (a21) from bottom to top, the post-oxidation gasification agents ( 36 ) brought in.

The post-oxidation process substances ( 35 ) are applied to the surface ( 10 ) of the forming post-oxidation bulk cone ( 11 ), whereby the post-oxidation moving bed (a22) is cooled. From the post-oxidation reaction space (a2), from the bottom to the top, the post oxidation oxidation dusts ( 37 ) laden post-oxidation raw gases ( 38 ) and from top to bottom over the ash discharge (a1) the cooled post-oxidation bottoms (C-free ashes) ( 39 ) deducted.

The solid gasification substances ( 25 ) are transported by the wall-like downflow by gravity predominantly into the zone of central fluidization (b112). From here, most of the solids are transported upwards and react at locally very high temperatures up to> 2,000 ° C with the laterally injected primary gasification gasifiers ( 27 ). The particle sizes of the carbonaceous gasification substances ( 25 ) and the liberated ashes melt and agglomerate to form fused agglomerates. Throughout the primary gasification reaction space (b1) there are so intense heat and mass transfer conditions that the incoming solid gasification substances ( 25 ) and the primary gasification process materials ( 26 ) are mixed and heated over the shortest route and the solid again heated by the oxidation reactions, solid gasification materials and molten ashes or melt agglomerates again and solidify. The extreme fluidization in the zone of central fluidization (b112) is achieved by high flow rates of the secondary gasification raw gas flowing up from the bottoms removal (b111). The flow rates, based on the free cross-section of the central product withdrawal (b111), are at 2-6 m / s and thus in the typical range for circulating fluidized beds. The height of the zone of central fluidization (b112) reaches - without the extension by the injection of the primary gasification gasification agent ( 27 ) - three times the diameter of the bottom product take-off (b111).

By injecting the primary gasification gasification agent ( 27 ) in the zone of central fluidization (b112) extends this up to about 6 times. Although the highest energy densities occur in the primary gasification reaction space (b11) as a result of the highly dominant, exothermic reactions of the partial oxidation, the high carbon concentrations of the circulating solids permanently ensure that the gasifier walls remain free from ashes or slag caking or slagging in the Flows of the bubble layer gasification occur.

The circulating flow of the central fluidized bubbler gasification around the zone of central fluidization (b112) is so strong that no additional gas supplies to the bottom ( 2 ) are required for fluidization.

The primary gasification soil products ( 30 ), sink in countercurrent to the connector tube raw gases ( 33 ), which flow upwards and develop a sifter, through the central bottoms removal (b111) into the connector tube reaction space (c1). The primary gasification soil products ( 30 ) consist mainly of coarser and heavier, ash-rich particles including the resulting ash agglomerates. As the temperatures of primary gasification bottoms ( 30 ) are significantly higher than those of countercurrent connector tube raw gases ( 33 ), found in the connector reaction space (c1) with cooling of the primary gasification bottoms ( 30 ) endothermic gasification reactions take place, ie the carbon contents of the downwardly emerging connector tube bottoms ( 34 ) are lower than those from the top entering primary gasification bottoms ( 30 ).

In the connector tube reaction space (c1) dominates the reactor principle of entrained flow gasification. Especially in the vicinity of the central upper post-oxidation gas outlet (a25), a further particle size and density separation takes place in favor of coarser and heavier ash-rich particles as feedstock for the post-oxidation moving bed (a22). The post-oxidized, landfillable almost C-free ashes are discharged at temperatures of about 400 ° C by means of rotary grate (a21) in the ash discharge (a1).

The centrally fluidized bubbling gasification in the primary gasification reaction space (b1) extends over the conical primary gasification reaction space (b11) into the cylindrical primary gasification reaction space (b12). Here the hot gas-solid jet and the large-scale solids recirculation flow pass into a highly expanded fluidized bed in which the flow rates and temperatures of the primary gasification dusts ( 28 ) loaded primary gasification crude gases ( 29 ) across the cross section and prevails the reactor principle of a fluidized bed gasification.

The bottom of the top into the secondary gasification reaction space (b2) withdrawn, hot primary gasification crude gases ( 29 ) containing carbon-rich primary gasification dusts ( 28 ) are the result of the predominantly occurring reactions of total oxidation to form CO ₂ and H ₂ O. They cool in the secondary gasification reaction space (b2) as a result of the endothermic, carbon-consuming gasification reactions to form CO and H ₂ from , At the upper end of the secondary gasification reaction space (b2), the decay temperatures of the endothermic gasification reactions at about 1100 ° C are reached. The particle sizes of primary gasification dusts ( 28 ) are reduced to the discharge grain diameter of the secondary gasification fine dust ( 23 ), with the secondary gasification raw gas ( 24 ) are withdrawn from the secondary gasification reaction space (b2), whereby the carbon contents decrease. To the specified, small discharge grain diameter of the secondary gasification fine dust ( 23 ) with values smaller than 0.1 mm, the average flow rates of the secondary gasification reaction dust (b2) withdrawn with secondary gasification fine dust ( 23 ) laden secondary gasification crude gases ( 24 ) set correspondingly low. They allow the largely complete carbon conversion over a short path length of the flow, ie at low overall height of the gasification reactor (v). In the secondary gasification reaction space (b2), the particle sizes decrease from bottom to top and the reactor principle of fluidized bed gasification predominates. This area will expanded so long that from the bottom up in the quench zone reaction space (b3) fine dust are deducted whose carbon contents specifically values up to about 50 wt .-%, so that a correspondingly shorter secondary gasification reaction space (b2) is realized. High carbon contents are desirable at high gasification temperatures as a so-called plaster carbon to avoid slagging or misplacing.

Above the secondary gasification reaction space (b2), a quench zone reaction space (b3) is arranged, the task of which is to feed quench water into the lower quench area (b31). 22 ). The amount of quench water to be injected is adjusted so that the temperatures above the quench zone reaction space (b3) are lowered to values below the critical ash sintering limits in the range of about 950 ° C. The injection takes place by means of several quench nozzles ( 12 ). The injected quench water ( 22 ) not only cool the fine dust. In the quench zone reaction space (b3), under the prevailing conditions of fluidized-bed gasification, the quench water also reacts with the carbon of the carbon-containing particulate matter in conditions of entrainment gasification, carbon monoxide, carbon dioxide and hydrogen being formed. From the homogenization zone (b32), the top of the crude gas outlet (b4) at the top of the primary gasification fluidized-bed gasifier (b) is filled with fine dusts ( 20 ) loaded, quenched and cooled raw gases ( 21 ) deducted. The quenching process is used to advantage for pollutant disposal.

The apparatus technical design of the sheath of the reaction chamber is in 1 not shown and includes, as usual for fixed-bed pressure reactors, a pressure vessel with water jacket and saturated steam generation and an inner shell with refractory lining.

In the following, the most important material and process data of the gasification reactor (v) for the production of synthesis gas are described, in which at a gasification pressure of 60 bar dried lignite with water contents of about 12% by mass and grain sizes of about 0-2 mm be gasified with oxygen and water vapor as a gasifying agent. The lignite used is characterized by high reaction capabilities, average ash melting temperatures of about 1,250 ° C, critical ash sintering limits of about 1,000 ° C and in dry ashing very fine-grained ashes with grain sizes <about 0.2 mm.

As a post-oxidation gasification agent ( 36 ) enter the post-oxidation reaction space (a2) 11 % of the total oxygen (post-oxidation oxygen) and 96% of the total gasification gas supplied. The oxygen loadings of the free cross section of the post-oxidation reaction space (a2) is about 200 Nm ³ / m ² , and the steam / O ₂ ratio is about 7 kg / m ³ (iN). The post-oxidised ashes of post-oxidation bottoms ( 39 ) are withdrawn with C contents <5% by mass and temperatures around 400 ° C. The with post-oxidation dusts ( 37 ) laden post-oxidation raw gases ( 38 ) enter the connector tube reaction space (c1) at temperatures around 900 ° C. As a primary gasification-gasification agent ( 27 ) enter into the primary gasification reaction space (b1) 89% of the total oxygen (primary gasification oxygen) and 4% of the total supplied gasification water vapor, wherein 1/3 of the primary gasification oxygen via the lower primary gasification gasification agent nozzle level ( 6 ) and 2/3 above the upper primary gasification-gasification agent nozzle level ( 7 ) are injected. In the mixture nozzles of the primary gasification oxygen is injected in a mixture with 5 vol .-% steam. Temperatures of 1,150-1,200 ° C are reached at the upper end of the primary gasification reaction space (b1), with approx. 62% of the gasification material ( 25 ) were implemented. In the secondary gasification reaction space (b2), gas flow rates of about 0.5 m / s and average gas residence times of about 5 s are established. At the upper end of the secondary gasification reaction space (b2) are gasification temperatures of about 1100 ° C. and a carbon conversion of about 85% of that in the gasification substance ( 25 ) contained carbon. Due to the additional C conversion in the post-oxidation reaction space (a2), a total carbon conversion of about 99.8% of that in the gasification reaction space (v) is achieved ( 25 ) contained carbon. The crude gas is cooled in the quench zone reaction space (b3) to a temperature of about 950 ° C.

LIST OF REFERENCE NUMBERS

v

gasification reactor

v1

Gasification reaction chamber

a

Post-oxidation fixed-bed gasifier

a1

ash discharge

a2

Post-oxidation reaction chamber

a21

rotary grate

a22

Post-oxidation moving bed

a23

Post-oxidation gas dome

a24

Post-oxidation process material entry

a25

central upper post-oxidation gas outlet

b

Primary gasification fluidized bed gasifier

b1

Primary gasification reaction chamber

b11

conical primary gasification reaction space

b111

 central soil product withdrawal

b112

 Zone of central fluidization

b12

cylindrical primary gasification reaction space

b13

Gasification material entries

b14

multi-part primary gasification-gasification agent entry

b15

Primary gasification process material entry

b2

Secondary gasification reaction chamber

b3

Quench zones reaction chamber

b31

lower quench area

B311

 Quenchdüsenebene

b32

upper homogenization range

b4

crude gas

c

connector pipe

c1

Connector tube reaction chamber

1

Head of primary gasification fluidized bed gasifier

2

Bottom of the primary gasification fluidized bed gasifier

3

two superimposed primary gasification-gasification agent nozzle planes

4

Primary gasification gasification agent nozzles

5

Inclination angle 15 °

6

Lower primary gasification gasification agent nozzle level

7

upper primary gasification gasification agent nozzle level

8th

Post-oxidation process material nozzles level

9

Post-oxidation process material nozzles

10

Surface of post-oxidation bulk cone

11

Post-oxidation of repose

12

quench nozzles

20

(C-containing) fine dusts

21

loaded raw gases

22

quench

23

Secondary gasification fine dust

24

loaded secondary gasification crude gases

25

gasification material

26

Primary gasification process material

27

Primary gasification gasification agent

28

Primary gasification dusts

29

loaded primary gasification crude gases

30

(C-containing) primary gasification soil products

32

Connector tube dust

33

loaded connector tube raw gases

34

Connector tube bottoms

35

Post-oxidation process materials

36

Post-oxidation gasification agent

37

Post-oxidation dusts

38

loaded post-oxidation raw gases

39

Post-oxidation bottoms (C-free ash)

40

Recirculating secondary gasification fine dust

41

Quench zones-fine dust

42

recirculating quench zone fine dust

QUOTES INCLUDE IN THE DESCRIPTION

This list of the documents listed by the applicant has been generated automatically and is included solely for the better information of the reader. The list is not part of the German patent or utility model application. The DPMA assumes no liability for any errors or omissions.

Cited patent literature

• DE 102007006982 B4 [0006, 0008, 0009]
• DE 102007006980 B4 [0007]
• DE 102007006981 B4 [0008, 0012]
• EP 1201731 A1 [0008, 0010]
• DE 4339973 C1 [0011]
• DE 102013107311 A1 [0013]

Claims (8)

Process for the production of synthesis, reduction and / or combustion gases from solid gasification substances with the aid of oxygen-containing gasification agents containing water vapor and optionally CO ₂ as endothermic gasification agent, at elevated pressures using fluidized bed gasification, by means of a gasification reactor (v) a gasification reaction space (v1) comprising from bottom to top a post-oxidation fixed-bed gasifier (a) with a pressure vessel having a post-oxidation reaction space (a2) for receiving a moving bed, with a ash discharge (a1) at the bottom of the post-oxidation fixed bed gasifier (a ), having a post-oxidation gasification agent feed, a compound reaction space, a primary gasification fluidized bed gasifier (b) having a primary gasification reaction space (b1) having a central fluidization zone (b112), a multi-part primary gasification gasification agent (b) b14), with several gasification substance entries n (b13), having a secondary gasification reaction space (b2), with a crude gas outlet (b4) at the head of the primary gasification fluidized bed gasifier (b), a) wherein the reaction space of the primary gasification fluidized bed gasifier (b) directly or via a connector tube with the connection between primary gasification fluidized-bed gasifier (b) and post-oxidation fixed bed gasifier (a) with respect to the reaction spaces of primary gasification fluidized-bed gasifier (b) and post-oxidation gasifier (b). B) the gasification reaction space (v1) forms an uninterrupted coherent reaction space in which the post-oxidation reaction space (a2) is connected to the primary gasification reaction space (b1) through the connection reaction space and from the ash discharge (a1) to the raw gas outlet (b4) is sufficient, c) wherein in the post-oxidation reaction space (a2) in the post-oxidation moving bed, the reactor principle of the fixed bed gasification in the connection reaction space predominantly the reactor principle of entrained flow gasification and in the primary gasification reaction chamber (b1), the reactor principle of the central-fluidized bubbler gasification, passing d) wherein the primary gasification of the registered solid gasification materials is carried out with primary gasification gasification agents in the stationary fluidized bed, circulating fluidized bed, jet fluidized bed or bubble layer, e) wherein the gasification of the fluidized bed gasification, in the secondary gasification reaction space (b2) f). The post-oxidation of the primary gasification withdrawn from the primary gasification C-containing primary gasification bottom products with post-oxidation gasification agents in the post-oxidation moving bed and partly gasified f) wherein the post-oxidation soil products formed as d g. the post-oxidation moving bed in the post-oxidation fixed-bed gasifier consists of a lower cylindrical part and an upper, constricting part, the upper end of which is at most up to and below the reoxidation moving bed h) wherein the gases rising upwardly from the post-oxidation moving bed are introduced at flow rates into the lower end of the connection to the primary gasification fluidized bed gasifier (b) which is at most are so large that the primary gasification bottoms forming the post-oxidation moving bed can fall from the top of the primary gasification fluidized bed gasifier through the compound into the post-oxidation moving bed, i) from the top of the compound up into the primary gasification fluidized bed gasifier Entering gases are introduced at flow rates which are at least so large that the primary gasification bottoms are fluidized above the top of the compound, j) wherein the amount of post-oxidation gasification agent introduced into the post-oxidation moving bed and the amount of the Post-oxidation post-bed down-cut post-oxidation bottoms are adjusted to complete the post-oxidation below the top of the cylindrical part of the moving bed, k) where the solid carbon-containing gasification materials are fed into gasification feedstock (b1) b13) are introduced at heights between the upper region of the conically expanding primary gasification reaction space (b11) and the lower region of the cylindrical primary gasification reaction space (b1), l) wherein the primary gasification gasification means are laterally and / or centrally by means of gasification sen ( 27 ) are introduced via the primary gasification-gasification agent entries (b14) to altitudes which are at least in the zone of central fluidization (b112) and which extend to the lower region of the cylindrical primary gasification reaction space (b1), m) the primary gasification gasification means be injected and the gasification agent jet jets are provided with flow pulses that they do not contact the opposing walls of the primary gasifier, and the gasification agent jets penetrate, but do not penetrate, the central fluidization zone (b112) and, in conjunction with the gases ascending from the post-oxidation moving bed, form a bubbler gasification from the central fluidization , A method according to claim 1, characterized in that the oxygen content of the post-oxidation gasification agent is adjusted so that in the oxidation zone of the post-oxidation moving bed at most a permanent sintering and / or a local and temporally limited melting of the ash, but no slagging occurs , A method according to claim 2 or 3, characterized in that 70-95% of the oxygen of the total supplied gasification agent with the primary gasification gasification agents (primary gasification oxygen) and 30 - 5% with the post-oxidation gasification means (post-oxidation oxygen) are introduced. Method according to one of claims 1 to 3, characterized in that above the secondary gasification reaction space (b2) via quench nozzles ( 12 ) such quench water ( 22 ) is injected so that the temperatures of the secondary gasification raw gas laden with secondary gasification fine dusts are lowered to values below the critical ash sintering limits. Gasification reactor for the production of synthesis, reduction and / or combustion gases from solid gasification materials with the aid of oxygen-containing gasification agents containing water vapor and optionally CO ₂ as endothermic gasification agent, at elevated pressures using fluidized bed gasification (primary gasification), with a Nachoxidations- Fixed-bed gasifier (a) having a pressure vessel with a post-oxidation reaction space (a2) for receiving a moving bed, with a rotary grate with Nachoxidations gasification supply with a ash discharge (a1) at the bottom of post-oxidation fixed bed gasifier (a), with a primary gasification Wirbelschichtvergaser (b) having a primary gasification reaction space (b1) with a zone for central fluidization (b112), with a secondary gasification reaction space (b2), with a raw gas outlet (b4) at the top of the primary gasification fluidized bed gasifier (b), with a multi-part primary gasification Gasoline entry (b14), with several Vergasungsstoffeinträge (b13), with a connection between Nachoxidations fixed bed gasifier (a) and primary gasification fluidized bed gasifier (b) as a direct connection or connection via a connector tube (c) for pressure-tight and uninterrupted connection of the reaction spaces of primary gasification fluidized bed gasifier (b) and post-oxidation Fixed-bed gasifier (a), wherein the connection between primary gasification fluidized-bed gasifier (b) and post-oxidation fixed-bed gasifier (a) has a smaller cross section than the reaction spaces of primary gasification fluidized bed gasifier (b) and post-oxidation fixed bed gasifier (a), the gasification substance entries (b13 ) are arranged and configured as inclined tube entries on the primary gasification fluidized-bed gasifier (b) such that the gasification substances are introduced into the marginal area of the primary gasification reaction space (b1), wherein the multi-part primary gasification-gasification agent entry (b14) contains several over the Scope in at least one plane, at the bottom of the primary gasification fluidized bed gasifier, equally distributed, downwardly inclined and on the primary gasification carburetor axis in the zone of central fluidization (b112) aligned primary gasification gasification agent nozzles ( 4 ), wherein the primary gasification-gasification agent entry (b14) with the primary gasification gasification agent nozzles (b14) 4 ) is designed so that the primary gasification gasifying agents are injected and the primary gasifying agent jets are provided with flow pulses that do not contact the opposed walls of the primary gasifier, and the primary gasifying agent jets penetrate into the zone of central fluidization (b112), but they do not penetrate and, in conjunction with the gases ascending from the post-oxidation moving bed, lead to the formation of a bubbling gasification from the zone of central fluidization. Gasification reactor according to claim 5, characterized in that at the post-oxidation gas dome (a23) of the post-oxidation fixed bed gasifier (a) additionally feeds ( 9 ) for post-oxidation process materials ( 35 ) are arranged. Gasification reactor according to claim 5 or 6, characterized in that when connecting the primary gasification fluidized bed gasifier (b) and the post-oxidation fixed-bed gasifier (a) via the connector pipe (c), the upper end flush in the bottom of the primary gasification fluidized bed gasifier (b) and the the lower end is flush or not flush in the post-oxidation gas dome (a23) of the post-oxidation fixed bed gasifier (a), the contour of the connector tube (c) being that of a cylinder or a tube flaring towards the upper end and / or the lower end, and wherein the length of the connector tube (c) is at least as large as its mean diameter. Gasification reactor according to one of claims 5 to 7, characterized in that the primary gasification Wirbelschichtvergaser (b) above of the secondary gasification reaction space (b2) has a quench zone reaction space (b3), in the quench nozzles ( 12 ) for the injection of quench water ( 22 ).

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