EP0182992A2 - Low energy process for producing synthesis gas with a high methane content - Google Patents

Low energy process for producing synthesis gas with a high methane content Download PDF

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Publication number
EP0182992A2
EP0182992A2 EP85111795A EP85111795A EP0182992A2 EP 0182992 A2 EP0182992 A2 EP 0182992A2 EP 85111795 A EP85111795 A EP 85111795A EP 85111795 A EP85111795 A EP 85111795A EP 0182992 A2 EP0182992 A2 EP 0182992A2
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EP
European Patent Office
Prior art keywords
gas
reactor
synthesis gas
regenerator
heated
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EP85111795A
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German (de)
French (fr)
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EP0182992B1 (en
EP0182992A3 (en
Inventor
Peter Dr.-Ing. Heinrich
Klaus Dr.-Ing. Knop
Friedbert Dr.-rer. nat. Rübe
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MAN Gutehoffnungshutte GmbH
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MAN Gutehoffnungshutte GmbH
MAN Maschinenfabrik Augsburg Nuernberg AG
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/463—Gasification of granular or pulverulent flues in suspension in stationary fluidised beds
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/02—Dust removal
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/04—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/093—Coal
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0959—Oxygen
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0973—Water
    • C10J2300/0976—Water as steam
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1671—Integration of gasification processes with another plant or parts within the plant with the production of electricity
    • C10J2300/1675—Integration of gasification processes with another plant or parts within the plant with the production of electricity making use of a steam turbine
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1861—Heat exchange between at least two process streams
    • C10J2300/1884—Heat exchange between at least two process streams with one stream being synthesis gas
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S48/00—Gas: heating and illuminating
    • Y10S48/01—Recirculation of gases produced to lower part of fuel bed

Definitions

  • the invention relates to a process for the production of synthesis gas, in which the synthesis gas obtained in a reactor by gasifying C-containing fuel is cooled in a regenerator and subjected to a gas treatment, and part of the gas as recycle gas is returned to the reactor together with combustion gas and C -containing fuel is supplied, the gas being heated by the regenerator before re-entering the reactor.
  • Patent 32 23 702 of the applicant discloses a method of the type mentioned for the production of synthesis gas. This process is characterized by low energy consumption since the high temperature energy of the gas emerging from the synthesis gas is used to heat the cycle gas before it re-enters the reactor.
  • the invention has for its object to provide a method for generating synthesis gas with a relatively high methane content, which has a particularly low energy consumption and can therefore be carried out particularly economically.
  • the process is also said to do without a conversion step and to provide a synthesis gas which is particularly suitable for direct ore reduction.
  • This object is achieved in a method according to the invention in that the gas is further cooled in the gas preparation in a 4-pole heat exchanger and a condenser, is subjected to a gas scrub to remove the main part of methane and carbon dioxide and after re-passage through the 4-pole heat exchanger is heated and fed to a heater
  • the raw gas is cooled to the extent that it passes below its dew point after passing through the regenerator in the 4-pole heat exchanger and the condenser.
  • the heat energy extracted from the gas is not dissipated, but is fed back into the circuit at the points where the heat energy is required.
  • the process enables a hydrogen-rich synthesis gas for the direct ore reduction to be prepared in a simple manner, methane also being obtained as a valuable by-product, which is used as synthesis gas for the production of chemical products, for example in the production of methanol, or as fuel gas for others Process can be used.
  • the synthesis gas can be conducted in such a way that after the first Passage passes through the heater by the 4 P ol heat exchanger.
  • the method further provides that oxygen is introduced as combustion gas into the gasification reactor.
  • oxygen is introduced as combustion gas into the gasification reactor.
  • the oxygen improves the gasification behavior of the coal. It is advantageous for the energy balance of the process if part of the excess process steam energy is used to generate oxygen for the reactor.
  • carbon is fed to a fluidized bed reactor 1 in the form of fine-grained, reactive coal dust.
  • Highly heated process steam, oxygen and cycle gas are passed into the reactor 1 as gasifying agents for the coal dust.
  • the composition of the cycle gas is shown in Table 1, column 3.0.
  • the coal is gasified at o a temperature of 800 C and a pressure of 10 bar.
  • the ash produced during coal gasification is withdrawn from the bottom of the reactor.
  • the synthesis raw gas leaves the reactor overhead with a composition according to column 4.0, table 1.
  • the raw gas After passing a fly ash or dust separator 2, the raw gas then enters the cooling element of a regenerator 3, in which it cools from 800 C to 578 C. becomes.
  • a regenerator 3 Suitable regenerators that extract heat from a hot gas stream via a cooling element, store it and transfer the storage heat to another gas stream via a heating element are known to the person skilled in the art, for. B. known from blast furnace technology and glass production and therefore do not need to be described in particular.
  • the gas is cooled further in a 4-pole heat exchanger 4 and a condenser 5, in which the gas is cooled down to 60.degree.
  • the condensate water accumulating in the condenser 5 is drained off.
  • the gas is subjected to a so-called PSA gas scrubbing at 6, through which the methane and carbon dioxide content of the synthesis gas is selectively separated from the gas stream.
  • PSA gas scrubbing is a known absorption process in which certain gases to be separated from a gas stream are absorbed by a solid and then by a purge gas, e.g. B. nitrogen, are removed after depressurization. The separated methane and carbon dioxide are removed from the gas cycle and are available for other use.
  • Gas scrubbing 6 significantly increases the hydrogen content of the synthesis gas, as can be seen in Table 1, column 6.0.
  • the synthesis gas now has the gas composition that is required for the later ore reduction.
  • the synthesis gas is fed to a compressor 7 and then passes through the 4-pole heat exchanger 4 again, in which it is heated to 466 ° C.
  • the gas stream passes through a heater 8, in which the process steam required in the process is additionally generated and in which the synthesis gas is heated to a high degree by burning part of the methane separated off in the gas scrubber 6, so that after passing through the heater 8 the synthesis gas enters the reduction reactor 9 at a temperature of 900 ° C.
  • the synthesis gas is partially oxidized during the reduction and then leaves the reactor 9 with a lower-hydrogen composition according to Table 1, column 3.0.
  • This so-called blast furnace gas is fed to the heating element of the regenerator 3 0, by means of which it is heated to 750 ° C. and is then re-introduced into the reactor 1 as a circulating gas.
  • the superheated steam generated in the heater 8 drives a steam turbine 10, the output of which covers practically the entire electrical energy requirement of the method. Part of the turbine power is used to produce the oxygen required in coal gasification by air separation at 11. The oxygen is then compressed and fed to the reactor 1.
  • the steam emerging from the steam turbine 10 is fed to the reactor 1 as process steam, it having previously been heated to 750 ° C. in the regenerator 3.
  • the top gas and process steam stream need not be conducted in separate lines, but can be combined before entering the regenerator 3 and heated together in the regenerator.

Abstract

Verfahren zur Erzeugung von Synthesegas, bei dem das in einem Reaktor (1) durch Vergasung von C-haltigem Brennmaterial gewonnene Synthesegas in einem Regenerator (3) abgekühlt und einer Gasaufbereitung (6) unterzogen wird, und ein Teil des Gases als Kreislaufgas dem Reaktor (1) wieder zusammen mit Brennstoff zugeführt wird, wobei das Gas vor dem Wiedereintrittt in den Reaktor von dem Regenerator (3) aufgeheizt wird, und bei dem bei der Gasaufbereitung das Synthesegas in einem 4-Pol-Wärmeaustauscher (4) und einem Kondensator (5) weiter abgekühlt wird, einer Gaswäsche (6) zur Entfernung des Hauptanteils von Methan und Kohlendioxid unterzogen wird und nach erneutem Durchtritt durch den 4-Pol-Wärmeaustauscher (4) aufgeheizt wird. Eine weitere Erhitzunger folgt in einem Gaserhitzer (8), wonach das Gas einem Erzreduktionsreaktor (9) zugeführt und nach Austritt aus dem Erzreduktionsreaktor (9) und nach erneutem Aufheizen in dem Regenerator (3) dem Vergasungsreaktor (1) wieder zugeführt wird. Der Methananteil des in dem Reaktor (1) erzeugten Synthesegases kann selektiv in der Gaswäsche (6) entfernt und zur Erzeugung chemischer Produckte verwendet werden.Process for the production of synthesis gas, in which the synthesis gas obtained in a reactor (1) by gasification of C-containing fuel is cooled in a regenerator (3) and subjected to a gas treatment (6), and part of the gas as recycle gas is passed to the reactor ( 1) is fed again together with fuel, the gas being heated by the regenerator (3) before it re-enters the reactor, and in which the synthesis gas is processed in a 4-pole heat exchanger (4) and a condenser (5 ) is cooled further, is subjected to a gas scrubbing (6) to remove the main part of methane and carbon dioxide and is heated after passing through the 4-pole heat exchanger (4) again. A further heater follows in a gas heater (8), after which the gas is fed to an ore reduction reactor (9) and, after exiting the ore reduction reactor (9) and after being heated again in the regenerator (3), is fed back to the gasification reactor (1). The methane content of the synthesis gas generated in the reactor (1) can be selectively removed in the gas scrubber (6) and used to produce chemical products.

Description

Die Erfindung betrifft ein Verfahren zur Erzeugung von Synthesegas, bei dem das in einem Reaktor durch Vergasung von C-haltigem Brennmaterial gewonnene Synthesegas in einem Regenerator abgekühlt und einer Gasaufbereitung unterzogen wird, und ein Teil des Gases als Kreislaufgas dem Reaktor wieder zusammen mit Verbrennungsgas und C-haltigen Brennmaterial zugeführt wird, wobei das Gas vor dem Wiedereintrittt in den Reaktor von dem Regenerator aufgeheizt wird.The invention relates to a process for the production of synthesis gas, in which the synthesis gas obtained in a reactor by gasifying C-containing fuel is cooled in a regenerator and subjected to a gas treatment, and part of the gas as recycle gas is returned to the reactor together with combustion gas and C -containing fuel is supplied, the gas being heated by the regenerator before re-entering the reactor.

Durch das Patent 32 23 702 der Anmelderin ist ein Verfahren der genannten Art zur Erzeugung von Synthesegas bekannt. Dieses Verfahren zeichnet sich durch einen niedrigen Energieverbrauch aus, da die Hochtemperaturenergie des aus dem Synthesegas austretenden Gases dafür verwendet wird, um das Kreislaufgas vor dem Wiedereintritt in den Reaktor aufzuheizen.Patent 32 23 702 of the applicant discloses a method of the type mentioned for the production of synthesis gas. This process is characterized by low energy consumption since the high temperature energy of the gas emerging from the synthesis gas is used to heat the cycle gas before it re-enters the reactor.

Unter den im Reaktor herrschenden Vergasungsbedingungen wird bei diesem Verfahren ein Rohgas erhalten, bei dem der Wasserstoffgehalt relativ niedrig liegt und das so gut wie kein Methan enthält. Um den Wasserstoffgehalt des Gases aufzubessern, ist es weiterhin erforderlich, das Gas durch einen Hochtemperatur-Konverter zu schicken.Under the gasification conditions prevailing in the reactor, a raw gas is obtained in this process, in which the hydrogen content is relatively low and which contains virtually no methane. In order to improve the hydrogen content of the gas, it is still necessary to send the gas through a high-temperature converter.

Der Erfindung liegt die Aufgabe zugrunde, ein Verfahren zur Erzeugung von Synthesegas mit einem relativ hohen Methangehalt anzugeben, das einen besonders niedrigen Energieverbrauch aufweist und daher besonders wirtschaftlich durchgeführt werden kann. Das Verfahren soll ferner ohne einen Konvertierungsschritt auskommen und ein Synthesegas liefern, das sich insbesondere für die Erzdirektreduktion gut eignet.The invention has for its object to provide a method for generating synthesis gas with a relatively high methane content, which has a particularly low energy consumption and can therefore be carried out particularly economically. The process is also said to do without a conversion step and to provide a synthesis gas which is particularly suitable for direct ore reduction.

Diese Aufgabe wird bei einem Verfahren gemäß der Erfindung dadurch gelöst, daß bei der Gasaufbereitung das Synthesegas in einem 4-Pol-Wärmetauscher und einem Kondensator weiter abgekühlt wird, einer Gaswäsche zur Entfernung des Hauptanteils von Methan und Kohlendioxid unterzogen wird und nach erneutem Durchtritt durch den 4-Pol-Wärmeaustauscher aufgeheizt einem Erhitzer zugeführt wird,This object is achieved in a method according to the invention in that the gas is further cooled in the gas preparation in a 4-pole heat exchanger and a condenser, is subjected to a gas scrub to remove the main part of methane and carbon dioxide and after re-passage through the 4-pole heat exchanger is heated and fed to a heater

und daß zumindest ein Teil des im Erhitzer zusätzlich gebildeten Prozeßdampfes dem Vergasungsreaktor zugeführt wird.and that at least part of the process steam additionally formed in the heater is fed to the gasification reactor.

Bei dem erfindungsgemäßen Verfahren wird das Rohgas nach Durchlaufen des Regenerators in dem 4-Pol-Wärmetauscher und dem Kondensator soweit abgekühlt, daß es seinen Taupunkt unterschreitet. Die dem Gas entzogene Wärmeenergie wird aber nicht abgeführt, sondern an den Stellen in den Kreislauf wieder eingespeist, an denen die Wärmeenergie benötigt wird. Durch das Verfahren läßt sich auf einfache Weise ein wasserstoffreic";;s Synthesegas für die Erzdirektreduktion darstellen, wobei als wertvolles Nebenprodukt auch noch Methan anfällt, das als Synthesegas zur Erzeugung chemischer Produkte, z. B. bei der Methanolerzeugung, oder als Brenngas bei anderen Verfahren eingesetzt werden kann.In the process according to the invention, the raw gas is cooled to the extent that it passes below its dew point after passing through the regenerator in the 4-pole heat exchanger and the condenser. However, the heat energy extracted from the gas is not dissipated, but is fed back into the circuit at the points where the heat energy is required. The process enables a hydrogen-rich synthesis gas for the direct ore reduction to be prepared in a simple manner, methane also being obtained as a valuable by-product, which is used as synthesis gas for the production of chemical products, for example in the production of methanol, or as fuel gas for others Process can be used.

Bei einer zweiten Variante des Verfahrens kann das Synthesegas derart geführt werden, daß es nach dem ersten Durchtritt durch den 4-Pol-Wärmeaustauscher den Erhitzer durchläuft.In a second variant of the method, the synthesis gas can be conducted in such a way that after the first Passage passes through the heater by the 4 P ol heat exchanger.

Bei dem Verfahren ist weiterhin vorgesehen, daß in den Vergasungsreaktor Sauerstoff als Verbrennungsgas eingeleitet wird. Zusammen mit dem Prozeßdampf, der die Reaktionsfähigkeit der im Reaktor eingesetzten Kohle steigert, wird durch den Sauerstoff das Vergasungsverhalten der Kohle verbessert. Vorteilhaft für die Energiebilanz des Verfahrens ist es, wenn ein Teil der im Überschuß anfallenden Prozeßdampfenergie zur Sauerstofferzeugung für den Reaktor eingesetzt wird.The method further provides that oxygen is introduced as combustion gas into the gasification reactor. Together with the process steam, which increases the reactivity of the coal used in the reactor, the oxygen improves the gasification behavior of the coal. It is advantageous for the energy balance of the process if part of the excess process steam energy is used to generate oxygen for the reactor.

Im folgenden wird anhand eines Schemas ein Ausführungsbeispiel des erfindungsgemäßen Verfahrens näher beschrieben. Die einzige Figur der Zeichnung zeigt ein Blockdiagramm einer Anlage zur Erzeugung von Synthesegas, mit dem ein Erzreduktionsreaktor beschickt wird.An exemplary embodiment of the method according to the invention is described in more detail below on the basis of a diagram. The only figure in the drawing shows a block diagram of a plant for generating synthesis gas, with which an ore reduction reactor is fed.

Gemäß der Figur wird einem Wirbelbett-Reaktor 1 Kohlenstoff in Form von feinkörnigem, reaktivem Kohlenstaub zugeführt. Als Vergasungsmittel für den Kohlenstaub werden hocherhitzter Prozeßdampf, Sauerstoff und Kreislaufgas in den Reaktor 1 geleitet. Die Zusammensetzung des Kreislaufgases ist aus Tabelle 1, Spalte 3.0 ersichtlich.According to the figure, carbon is fed to a fluidized bed reactor 1 in the form of fine-grained, reactive coal dust. Highly heated process steam, oxygen and cycle gas are passed into the reactor 1 as gasifying agents for the coal dust. The composition of the cycle gas is shown in Table 1, column 3.0.

In dem Reaktor 1 erfolgt die Vergasung der Kohle bei o einer Temperatur von 800 C und einem Druck von 10 bar. Die bei der Kohlevergasung anfallende Asche wird unten aus dem Reaktor abgezogen. Das Synthese-Rohgas verläßt den Reaktor über Kopf mit einer Zusammensetzung gemäß Spalte 4.0, Tabelle 1.In the reactor 1, the coal is gasified at o a temperature of 800 C and a pressure of 10 bar. The ash produced during coal gasification is withdrawn from the bottom of the reactor. The synthesis raw gas leaves the reactor overhead with a composition according to column 4.0, table 1.

Nach Passieren eines Flugasche- oder Staubabscheiders 2 tritt das Rohgas dann in das Kühlelement eines Regenerators 3 ein, in dem es von 800 C auf 578 C abgekühlt wird. Geeignete Regeneratoren, die über ein Kühlelement einem heißen Gasstrom Wärme entziehen, speichern und über ein Heizelement die Speicherwärme auf einen anderen Gasstrom übertragen, sind dem Fachmann z. B. aus der Hochofentechnik und der Glasherstellung bekannt und brauchen daher nicht besonders beschrieben zu werden. Eine weitere Abkühlung erfährt das Gas in einem 4-Pol-Wärmeaustauscher 4 und einem Kondensator 5, in dem das 0 Gas bis auf 60 C abgekühlt wird. Das im Kondensator 5 anfallende Kondensatwasser wird abgeleitet.After passing a fly ash or dust separator 2, the raw gas then enters the cooling element of a regenerator 3, in which it cools from 800 C to 578 C. becomes. Suitable regenerators that extract heat from a hot gas stream via a cooling element, store it and transfer the storage heat to another gas stream via a heating element are known to the person skilled in the art, for. B. known from blast furnace technology and glass production and therefore do not need to be described in particular. The gas is cooled further in a 4-pole heat exchanger 4 and a condenser 5, in which the gas is cooled down to 60.degree. The condensate water accumulating in the condenser 5 is drained off.

Im Anschluß an den Kondensator 5 wird das Gas einer sogenannten PSA-Gaswäsche bei 6 unterzogen, durch die der Methan- und Kohlendioxid-Anteil des Synthesegases selektiv aus dem Gasstrom abgetrennt wird. Bei dieser Gaswäsche handelt es sich um ein bekanntes Absorbtionsverfahren, bei dem bestimmte, aus einem Gasstrom abzutrennende Gase an einem Feststoff absorbiert und anschließend durch ein Spülgas, z. B. Stickstoff, nach Druckentspannung entfernt werden. Das abgetrennte Methan und das Kohlendioxid werden aus dem Gaskreislauf ausgeschelust und stehen zur anderweitigen Verwendung zur Verfügung.Following the condenser 5, the gas is subjected to a so-called PSA gas scrubbing at 6, through which the methane and carbon dioxide content of the synthesis gas is selectively separated from the gas stream. This gas scrubbing is a known absorption process in which certain gases to be separated from a gas stream are absorbed by a solid and then by a purge gas, e.g. B. nitrogen, are removed after depressurization. The separated methane and carbon dioxide are removed from the gas cycle and are available for other use.

Durch die Gaswäsche 6 wird der Wasserstoffgehalt des Synthesegases erheblich heraufgesetzt, wie aus Tabelle 1, Spalte 6.0 ersichtlich ist. Das Synthesegas hat jetzt die Gaszusammensetzung, die für die spätere Erzreduktion benötigt wird.Gas scrubbing 6 significantly increases the hydrogen content of the synthesis gas, as can be seen in Table 1, column 6.0. The synthesis gas now has the gas composition that is required for the later ore reduction.

Im Anschluß an die Gaswäsche 6 wird das Synthesegas einem Kompressor 7 zugeführt und durchläuft danach erneut den 4-Pol-Wärmeaustauscher 4, in welchem es auf 466° C aufgeheizt wird. Bevor das Gas dann in einen Reduktionsreaktor 9 eingeleitet wird, durchläuft der Gasstrom einen Erhitzer 8, in dem zusätzlich der bei dem Verfahren benötigte Prozeßdampf erzeugt wird und in dem das Synthesegas durch Verbrennen eines Teils des bei der Gaswäsche 6 abgetrennten Methans hoch erhitzt wird, daß nach Durchlaufen des Erhitzers 8 das Synthesegas mit einer Temperatur von 900° C in den Reduktionsreaktor 9 eintritt.Following the gas scrubbing 6, the synthesis gas is fed to a compressor 7 and then passes through the 4-pole heat exchanger 4 again, in which it is heated to 466 ° C. Before the gas is then introduced into a reduction reactor 9, the gas stream passes through a heater 8, in which the process steam required in the process is additionally generated and in which the synthesis gas is heated to a high degree by burning part of the methane separated off in the gas scrubber 6, so that after passing through the heater 8 the synthesis gas enters the reduction reactor 9 at a temperature of 900 ° C.

In dem Reduktionsreaktor 9, in dem Eisenerz direkt zu Eisenschwamm reduziert wird, wird das Synthesegas bei der Reduktion teilweise oxidiert und verläßt anschliessend den Reaktor 9 mit einer wasserstoffärmeren Zusammensetzung gemäß Tabelle 1, Spalte 3.0. Dieses sogenannte Gichtgas wird dem Heizelement des Regenerators 3 0 zugeführt, durch das es auf 750 C aufgeheizt wird und anschließend hocherhitzt als Kreislaufgas wieder in den Reaktor 1 eingeleitet wird.In the reduction reactor 9, in which iron ore is reduced directly to sponge iron, the synthesis gas is partially oxidized during the reduction and then leaves the reactor 9 with a lower-hydrogen composition according to Table 1, column 3.0. This so-called blast furnace gas is fed to the heating element of the regenerator 3 0, by means of which it is heated to 750 ° C. and is then re-introduced into the reactor 1 as a circulating gas.

Der im Erhitzer 8 erzeugte hocherhitzte Wasserdampf treibt eine Dampfturbine 10 an, deren Leistung praktisch den gesamten elektrischen Energiebedarf des Verfahrens deckt. Ein Teil der Turbinenleistung wird dazu verwendet, den bei der Kohle-Vergasung benötigten Sauerstoff durch Luftzerlegung bei 11 herzustellen. Der Sauerstoff wird anschließend komprimiert und dem Reaktor 1 zugeführt.The superheated steam generated in the heater 8 drives a steam turbine 10, the output of which covers practically the entire electrical energy requirement of the method. Part of the turbine power is used to produce the oxygen required in coal gasification by air separation at 11. The oxygen is then compressed and fed to the reactor 1.

Der aus der Dampfturbine 10 austretende Dampf wird als Prozeßdampf dem Reaktor 1 zugeführt, wobei er zuvor im o Regenerator 3 auf 750 C aufgeheizt wird. Dadurch, daß zusätzlich zum Gichtgas auch der Prozeßdampf im Regenerator 3 aufgeheizt wird, wird die Energiebilanz des Verfahrens weiterhin verbessert. Selbstverständlich brauchen der Gichtgas- und Prozeßdampfstrom nicht in getrennten Leitungen geführt zu werden, sondern können vor dem Eintritt in den Regenerator 3 vereinigt und gemeinsam in dem Regenerator aufgeheizt werden.The steam emerging from the steam turbine 10 is fed to the reactor 1 as process steam, it having previously been heated to 750 ° C. in the regenerator 3. The fact that in addition to the blast furnace gas also heats the process steam in the regenerator 3, the energy balance of the process is further improved. Of course, the top gas and process steam stream need not be conducted in separate lines, but can be combined before entering the regenerator 3 and heated together in the regenerator.

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Vorgegebene VerfahrensdatenSpecified process data

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Claims (7)

1. Verfahren zur Erzeugung von Synthesegas, bei dem das in einem Reaktor durch Vergasung von C-haltigem Brennmaterial gewonnene Synthesegas in einem Regenerator abgekühlt und einer Gasaufbereitung unterzogen wird, und ein Teil des Gases als Kreislaufgas dem Reaktor wieder zusammen mit Verbrennungsgas und C-haltigem Brennmaterial zugeführt wird, wobei das Gas vor dem Wiedereintrittt in den Reaktor von dem Regenerator aufgeheizt wird,
dadurch gekennzeichnet, daß
bei der Gasaufbereitung das Synthesegas in einem 4-Pol-Wärmetauscher (4) und einem Kondensator (5) weiter abgekühlt wird, einer Gaswäsche (6) zur Entfernung des Hauptanteils von Methan und Kohlendioxid unterzogen wird und nach erneutem Durchtritt durch den 4-Pol-Wärmeaustauscher (4) aufgeheizt einem Erhitzer (8) zugeführt wird, und daß zumindest ein Teil des im Erhitzer (8) gebildeten Prozeßdampf dem Vergasungsreaktor (1) zugeführt wird.1. A process for the production of synthesis gas, in which the synthesis gas obtained in a reactor by gasification of C-containing fuel is cooled in a regenerator and subjected to a gas treatment, and part of the gas as recycle gas is returned to the reactor together with combustion gas and C-containing Fuel is supplied, the gas being heated by the regenerator before re-entering the reactor,
characterized in that
during the gas treatment, the synthesis gas is further cooled in a 4-pole heat exchanger (4) and a condenser (5), is subjected to a gas scrubbing (6) to remove the main part of methane and carbon dioxide and after passing through the 4-pole Heat exchanger (4) is heated to a heater (8), and that at least part of the process steam formed in the heater (8) is fed to the gasification reactor (1). 2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß das Synthesegas nach dem ersten Durchtritt durch den 4-Pol-Wärmeaustauscher (4) den Erhitzer (8) durchläuft.2. The method according to claim 1, characterized in that the synthesis gas after the first passage through the 4-pole heat exchanger (4) passes through the heater (8). 3. Verfahren nach Anspruch 1 oder 2, dadurch gekennzeichnet, daß das Synthesegas im Anschluß an die Gasaufbereitung in einem Erzreduktionsreaktor (9) partiell oxidiert wird.3. The method according to claim 1 or 2, characterized in that the synthesis gas is partially oxidized in an ore reduction reactor (9) following the gas processing. 4. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß in den Vergasungsreaktor (1) Sauerstoff als Verbrennungsgas eingeleitet wird.4. The method according to claim 1, characterized in that oxygen is introduced as the combustion gas in the gasification reactor (1). 5. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß ein Teil der Prozeßdampfenergie zur Sauerstofferzeugung für den Reaktor (1) eingesetzt wird.5. The method according to claim 1, characterized in that part of the process steam energy is used to generate oxygen for the reactor (1). 6. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß in der Gaswäsche (6) der Methan-Anteil des in dem Vergasungsreaktor (1) erzeugten Synthesegases selektiv entfernt und aus dem Gaskreislauf zur anderweitigen Verwendung ausgeschleust wird.6. The method according to claim 1, characterized in that in the gas scrubbing (6) the methane portion of the synthesis gas generated in the gasification reactor (1) is selectively removed and discharged from the gas cycle for other use. 7. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß der im Erhitzer (8) gebildete Prozeßdampf vor dem Eintritt in den Vergasungsreaktor (1) durch den Regenerator (3) aufgeheizt wird.7. The method according to claim 1, characterized in that the process steam formed in the heater (8) is heated by the regenerator (3) before entering the gasification reactor (1).
EP85111795A 1984-10-27 1985-09-18 Low energy process for producing synthesis gas with a high methane content Expired EP0182992B1 (en)

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AU4786585A (en) 1986-05-01
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EP0182992B1 (en) 1988-11-02
IN166503B (en) 1990-05-19
US4678480A (en) 1987-07-07
DE3439487A1 (en) 1986-06-26
AU578312B2 (en) 1988-10-20
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BR8505349A (en) 1986-08-05

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