EP2981596A1 - Method for producing synthesis gas for conversion to products - Google Patents

Method for producing synthesis gas for conversion to products

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Publication number
EP2981596A1
EP2981596A1 EP14714167.5A EP14714167A EP2981596A1 EP 2981596 A1 EP2981596 A1 EP 2981596A1 EP 14714167 A EP14714167 A EP 14714167A EP 2981596 A1 EP2981596 A1 EP 2981596A1
Authority
EP
European Patent Office
Prior art keywords
synthesis gas
reformer
conversion
pure
crude
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP14714167.5A
Other languages
German (de)
French (fr)
Inventor
Karl-Heinz Jass
Ralf Abraham
Dobrin Toporov
Domenico PAVONNE
Max Heinritz-Adrian
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
ThyssenKrupp Industrial Solutions AG
Original Assignee
ThyssenKrupp Industrial Solutions AG
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by ThyssenKrupp Industrial Solutions AG filed Critical ThyssenKrupp Industrial Solutions AG
Publication of EP2981596A1 publication Critical patent/EP2981596A1/en
Withdrawn legal-status Critical Current

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Classifications

    • 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
    • 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
    • C10J2300/0956—Air or oxygen enriched air
    • 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
    • C10J2300/164—Integration of gasification processes with another plant or parts within the plant with conversion of synthesis gas
    • C10J2300/1656—Conversion of synthesis gas to chemicals
    • C10J2300/1659—Conversion of synthesis gas to chemicals to liquid hydrocarbons
    • 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
    • C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water

Definitions

  • the invention relates to a process for the production of synthesis gas for the conversion into products, in particular for synthesis gas liquefaction.
  • a carbonaceous fuel such as biomass or coal
  • a reactor in which the carbonaceous fuel with air or oxygen or oxygen-enriched air and with water vapor and carbon dioxide by gasification, for example by entrained flow gasification, fluidized bed gasification or other gasification methods (eg fixed bed gasification, etc.) is reacted at elevated temperature, preferably at temperatures between 800 to 1200 ° C or higher, to a crude synthesis gas consisting essentially of hydrogen, carbon dioxide and carbon monoxide.
  • the crude synthesis gas produced is cleaned by play, for example chlorine, pivoting ⁇ FEL-, carbon dioxide and dust particles are removed by filtration, chemical / physical processes from the raw synthesis gas.
  • the gereinig ⁇ te raw synthesis gas to a synthesis gas conversion is supplied, for example, generated based on the Fischer-Tropsch synthesis or methanol synthesis, the final liquid product.
  • Synthesis gas conversion technology such as syngas liquefaction
  • a high-quality gas ie, a gas of pure CO and H2.
  • the crude synthesis gas always also has proportions of methane, whereby experience has shown that the content of methane in the crude synthesis gas is about 4 to 10%.
  • this object is achieved according to the invention in that the exhaust gas generated in the process of conversion is converted into pure synthesis gas and this is fed into the purified main synthesis gas stream.
  • the core idea of the invention is to integrate an additional cycle with a converted pure synthesis gas into the process, i. for example converting the offgas produced during the liquefaction process in the syngas liquefaction system into pure synthesis gas and, in turn, feeding the generated pure syngas into the main syngas stream.
  • a converted pure synthesis gas into the process, i. for example converting the offgas produced during the liquefaction process in the syngas liquefaction system into pure synthesis gas and, in turn, feeding the generated pure syngas into the main syngas stream.
  • the conversion of the produced exhaust gas into pure synthesis gas and the introduction of the pure synthesis gas into the main synthesis gas stream are preferably carried out more than once, ie, ideally, almost all of the exhaust gas has been converted.
  • a reformer for the conversion of the ex ⁇ gas is expediently a reformer, and especially an autothermal reformer or catalytic reformer provided.
  • An advantageous embodiment of the invention provides that the reformer of the synthesis gas conversion device is connected downstream.
  • the system for carrying out the method according to the invention is essentially formed by the contact elements reactor 6, synthesis cleaning device 7, synthesis gas conversion device 8 and reformer 9, which is in the form of an autothermal reformer.
  • the device 8 is arranged between the synthesis gas purification device 7 and the reformer 9.
  • the process begins with carbonaceous fuel 1, such as biomass, gases, liquids or coal, being fed to the reactor 6, where the carbonaceous fuel 1 is reacted with air or oxygen and with steam and carbon dioxide to form a crude synthesis gas 2.
  • the reaction is carried out by gasification, such as entrained flow gasification, fixed bed gasification or fluidized bed gasification and is at elevated temperature, which may be between 800 to 1200 ° C and higher.
  • the reacted crude synthesis gas 2 which consists essentially of hydrogen, carbon dioxide and carbon monoxide, is fed to the synthesis gas purifier 7 together with methane produced in the gasification in the reactor 6 in the course of a further process step in order to be purified there.
  • the purification of the crude synthesis gas 2 in the synthesis gas purification device 7 is carried out in a conventional manner, such as by filtering and chemical / physical processes.
  • portions of chlorine, sulfur, carbon dioxide and dust are removed from the crude synthesis gas 2, so that as a result a purified main synthesis gas stream 3 is removed arises, but still has additional shares of methane.
  • the next process step envisages, as further shown in FIG. 1, that the main synthesis gas stream 3 is conducted into the synthesis gas conversion device 8.
  • the synthesis gas liquefaction is carried out in a conventional manner, for example on the basis of Fischer-Tropsch synthesis or methanol synthesis, to produce the end product 10.
  • the resulting in the synthesis gas liquefaction 4 such as carbon monoxide, hydrogen, methane and higher hydrocarbons now together with methane via an additional circuit first in one of the synthesis gas conversion device 8 downstream reformer 9, in the embodiment shown in Fig. 1 as autothermal Reformer present, then passed to be converted into a pure synthesis gas 5.
  • the pure synthesis gas 5 is in turn fed to the main synthesis gas stream 3 guided into the synthesis gas conversion device 8.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Hydrogen, Water And Hydrids (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

The invention relates to a method for producing synthesis gas for conversion to products, in particular for synthesis gas liquefaction. In order to develop the method further in such a manner that an increase in the synthesis gas production is achieved, the following method steps are carried out: a) feeding a carbon-containing fuel (1) into a reactor (6) in which the fuel (1) is converted to a crude synthesis gas (2); b) purifying the crude synthesis gas (2), wherein the purified synthesis gas (2) with resulting methane is fed as main synthesis gas flow (3) to the synthesis gas conversion, during which an exhaust gas (4) is also produced; c) converting the produced exhaust gas (4) into a pure synthesis gas (5) and feeding the pure synthesis gas into the main synthesis gas flow (3).

Description

für die Umsetzung zu Produkten for the conversion to products
Die Erfindung betrifft ein Verfahren zur Herstellung von Synthesegas für die Umsetzung zu Produkten, insbesondere für die Synthesegasverflüssigung. The invention relates to a process for the production of synthesis gas for the conversion into products, in particular for synthesis gas liquefaction.
Verfahren der eingangs genannten Art sind aus dem Stand der Technik bekannt. Methods of the type mentioned are known from the prior art.
Hierzu wird ein kohlenstoffhaltiger Brennstoff, wie beispielsweise Biomasse oder Kohle, einem Reaktor zugeführt, in dem der kohlenstoffhaltige Brennstoff mit Luft oder Sauerstoff bzw. sauerstoffangereicherter Luft sowie mit Wasserdampf und Kohlendioxid mittels Vergasung, beispielsweise durch Flugstromvergasung, Wirbelschichtvergasung oder anderen Vergasungsmethoden (z.B. Festbettvergasung u.s.w.) bei erhöhter Temperatur, vorzugsweise bei Temperaturen zwischen 800 bis 1200°C oder höher, zu einem rohen Synthesegas umgesetzt wird, das zu einem wesentlichen Teil aus Wasserstoff, Kohlendioxid und Kohlenmonoxid besteht. For this purpose, a carbonaceous fuel, such as biomass or coal, fed to a reactor in which the carbonaceous fuel with air or oxygen or oxygen-enriched air and with water vapor and carbon dioxide by gasification, for example by entrained flow gasification, fluidized bed gasification or other gasification methods (eg fixed bed gasification, etc.) is reacted at elevated temperature, preferably at temperatures between 800 to 1200 ° C or higher, to a crude synthesis gas consisting essentially of hydrogen, carbon dioxide and carbon monoxide.
In einem weiteren Schritt des Verfahrens der eingangs genannten Art wird das erzeugte rohe Synthesegas gereinigt, indem Anteile, beispielsweise Chlor-, Schwe¬ fel-, Kohlendioxid- und Staubteile, durch Filterung, chemischen/physikalischen Prozessen aus dem rohen Synthesegas entfernt werden. Danach wird das gereinig¬ te rohe Synthesegas einer Synthesegasumsetzung zugeführt, die beispielsweise auf Grundlage der Fischer-Tropsch-Synthese oder Methanol-Synthese das flüssige Endprodukt erzeugt. In a further step of the method of the aforementioned kind, the crude synthesis gas produced is cleaned by play, for example chlorine, pivoting ¬ FEL-, carbon dioxide and dust particles are removed by filtration, chemical / physical processes from the raw synthesis gas. Thereafter, the gereinig ¬ te raw synthesis gas to a synthesis gas conversion is supplied, for example, generated based on the Fischer-Tropsch synthesis or methanol synthesis, the final liquid product.
Die Technologie der Synthesegasumsetzung, wie beispielsweise die Synthesegasverflüssigung, erfordert in der Regel ein qualitativ hochwertiges Gas, d.h. ein Gas aus reinem CO und H2. Hierbei ergibt sich jedoch die Problematik, dass bei Verfahren der eingangs genannten Art das rohe Synthesegas immer auch Anteile von Methan aufweist, wobei erfahrungsgemäß der Gehalt des Methans in dem rohen Synthesegas ca. 4 bis 10 % beträgt. Dies bedeutet, dass eine nahezu vollständige Erzeugung von reinem Synthesegas, d.h. Gas aus reinem CO und H2, nicht gegeben ist, was wiederum dazu führt, dass ein nicht geringer Betrag von chemischer Energie weiterhin in dem Methan, aber auch in höheren Kohlenwasserstoffen ge- speichert ist, was zur Folge hat, dass die Effizienz des gesamten Prozesses der Gasverflüssigung eine Beeinträchtigung erfährt. Synthesis gas conversion technology, such as syngas liquefaction, typically requires a high-quality gas, ie, a gas of pure CO and H2. However, this results in the problem that, in the process of the type mentioned, the crude synthesis gas always also has proportions of methane, whereby experience has shown that the content of methane in the crude synthesis gas is about 4 to 10%. This means that nearly complete production of pure synthesis gas, ie pure CO and H2 gas, is not present, which in turn results in a not inconsiderable amount of chemical energy remaining in the methane but also in higher hydrocarbons. stores, with the result that the efficiency of the entire process of gas liquefaction is impaired.
Hier setzt die Erfindung an, deren Aufgabe darin besteht, das Verfahren der eingangs genannten Art derart weiterzuentwickeln, dass eine Steigerung der Synthesegasproduktion erzielt wird. This is where the invention, whose task is to further develop the method of the type mentioned in such a way that an increase in the synthesis gas production is achieved.
Mit einem Verfahren der eingangs bezeichneten Art wird diese Aufgabe gemäß der Erfindung dadurch gelöst, dass das im Prozess der Umsetzung erzeugte Abgas in reines Synthesegas konvertiert wird und dieses in den gereinigten Hauptsynthesegasstrom zugeführt wird. With a method of the type described, this object is achieved according to the invention in that the exhaust gas generated in the process of conversion is converted into pure synthesis gas and this is fed into the purified main synthesis gas stream.
Vorteilhafte Ausgestaltungen der Erfindung ergeben sich aus den Unteransprüchen. Advantageous embodiments of the invention will become apparent from the dependent claims.
Kernidee der Erfindung ist es, einen zusätzlichen Kreislauf mit einem konvertierten reinen Synthesegas in das Verfahren zu integrieren, d.h. zum Beispiel das während des Prozesses der Verflüssigung in dem Synthesegasverflüssigungssystem produzierte Abgas in reines Synthesegas zu konvertieren und das erzeugte reine Synthesegas wiederum in den Hauptsynthesegasstrom zuzuführen. Dadurch, dass zusätzlich reines Synthesegas in den Hauptsynthesegasstrom geführt wird, wird vorteilhafterweise erreicht, dass ein höherer Anteil an gereinigtem Synthesegas über den Hauptsynthesegasstrom in die Synthesegasverflüssigungsvorrichtung gelangt, was wiederum zu einer erhöhten Produktion des gewünschten Flüssigkeitsproduktes und somit auch zu einer höheren Effizienz des gesamten Verfahrens führt. The core idea of the invention is to integrate an additional cycle with a converted pure synthesis gas into the process, i. for example converting the offgas produced during the liquefaction process in the syngas liquefaction system into pure synthesis gas and, in turn, feeding the generated pure syngas into the main syngas stream. By additionally conducting pure synthesis gas into the main synthesis gas stream, it is advantageously achieved that a higher proportion of purified synthesis gas passes into the synthesis gas liquefying apparatus via the main synthesis gas stream, which in turn leads to an increased production of the desired liquid product and thus to a higher efficiency of the entire process leads.
Da mit dem Prozess beispielsweise der Synthesegasverflüssigung fortlaufend die Produktion von Abgas einhergehen kann, erfolgt vorzugsweise die Konvertierung des produzierten Abgases in reines Synthesegas und die Zuführung des reinen Synthesegases in den Hauptsynthesegasstrom mehr als einmal, d.h. im Idealfall bis nahezu sämtliches Abgas konvertiert worden ist. Für die Konvertierung des Ab¬ gases ist zweckmäßigerweise ein Reformer, und hier insbesondere ein autothermer Reformer oder katalytischer Reformer, vorgesehen. Eine vorteilhafte Ausgestaltung der Erfindung sieht dabei vor, dass der Reformer der Synthesegasumsetzungsvorrichtung nachgeschaltet ist. Since the process of, for example, the synthesis gas liquefaction may be accompanied by the production of exhaust gas, the conversion of the produced exhaust gas into pure synthesis gas and the introduction of the pure synthesis gas into the main synthesis gas stream are preferably carried out more than once, ie, ideally, almost all of the exhaust gas has been converted. For the conversion of the ex ¬ gas is expediently a reformer, and especially an autothermal reformer or catalytic reformer provided. An advantageous embodiment of the invention provides that the reformer of the synthesis gas conversion device is connected downstream.
Weitere Vorteile, Merkmale und Einzelheiten der Erfindung ergeben sich aufgrund der nachfolgenden Beschreibung sowie anhand der Zeichnung. Diese zeigt in der einzigen Figur ein Schaltbild mit Prozessfluss zur Durchführung des erfindungsgemäßen Verfahrens. Further advantages, features and details of the invention will become apparent from the following description and from the drawing. This shows in the single figure a circuit diagram with process flow for carrying out the method according to the invention.
Die Anlage zur Durchführung des erfindungsgemäßen Verfahrens wird im Wesentlichen von den Anlageelementen Reaktor 6, Synthesereinigungsvorrichtung 7, Syn- thesegasumsetzungsvorrichtung 8 sowie Reformer 9, der in Gestalt eines au- tothermen Reformers vorliegt, gebildet. Die Vorrichtung 8 ist dabei zwischen der Synthesegasreinigungsvorrichtung 7 und dem Reformer 9 angeordnet. The system for carrying out the method according to the invention is essentially formed by the contact elements reactor 6, synthesis cleaning device 7, synthesis gas conversion device 8 and reformer 9, which is in the form of an autothermal reformer. The device 8 is arranged between the synthesis gas purification device 7 and the reformer 9.
Das Verfahren beginnt damit, dass kohlenstoffhaltiger Brennstoff 1, wie Biomasse, Gase, Flüssigkeiten oder Kohle, dem Reaktor 6 zugeführt wird, in dem der kohlenstoffhaltige Brennstoff 1 mit Luft oder Sauerstoff sowie mit Wasserdampf und Kohlendioxid zu einem rohen Synthesegas 2 umgesetzt wird. Die Umsetzung erfolgt mittels Vergasung, wie Flugstromvergasung, Festbettvergasung oder Wirbelschichtvergasung und wird bei erhöhter Temperatur, die zwischen 800 bis 1200° C und höher liegen kann. The process begins with carbonaceous fuel 1, such as biomass, gases, liquids or coal, being fed to the reactor 6, where the carbonaceous fuel 1 is reacted with air or oxygen and with steam and carbon dioxide to form a crude synthesis gas 2. The reaction is carried out by gasification, such as entrained flow gasification, fixed bed gasification or fluidized bed gasification and is at elevated temperature, which may be between 800 to 1200 ° C and higher.
Das umgesetzte rohe Synthesegas 2, das zu einem wesentlichen Teil aus Wasserstoff, Kohlendioxid und Kohlenmonoxid besteht, wird im Rahmen eines weiteren Verfahrensschrittes zusammen mit bei der Vergasung in dem Reaktor 6 erzeugtem Methan der Synthesegasreinigungsvorrichtung 7 zugeführt, um dort gereinigt zu werden. Die Reinigung des rohen Synthesegases 2 in der Synthesegasreinigungs- vorrichtung 7 erfolgt in herkömmlicher Weise, wie durch Filterung und chemische/physikalische Prozesse. Insbesondere werden im Rahmen des Reinigungsprozesses Anteile von Chlor, Schwefel, Kohlendioxid und Staub aus dem rohen Synthesegas 2 entfernt, so dass als Ergebnis ein gereinigter Hauptsynthesegasstrom 3 entsteht, der jedoch weiterhin zusätzliche Anteile von Methan aufweist. The reacted crude synthesis gas 2, which consists essentially of hydrogen, carbon dioxide and carbon monoxide, is fed to the synthesis gas purifier 7 together with methane produced in the gasification in the reactor 6 in the course of a further process step in order to be purified there. The purification of the crude synthesis gas 2 in the synthesis gas purification device 7 is carried out in a conventional manner, such as by filtering and chemical / physical processes. In particular, in the course of the purification process, portions of chlorine, sulfur, carbon dioxide and dust are removed from the crude synthesis gas 2, so that as a result a purified main synthesis gas stream 3 is removed arises, but still has additional shares of methane.
Der nächste Verfahrensschritt sieht vor, wie aus Fig. 1 weiter hervorgeht, dass der Hauptsynthesegasstrom 3 in die Synthesegasumsetzungsvorrichtung 8 geleitet wird. The next process step envisages, as further shown in FIG. 1, that the main synthesis gas stream 3 is conducted into the synthesis gas conversion device 8.
In der Synthesegasumsetzungsvorrichtung 8 wird in herkömmlicher Weise, beispielsweise auf Basis der Fischer-Tropsch-Synthese oder Methanol-Synthese, die Synthesegasverflüssigung vollzogen, um das Endprodukt 10 zu erzeugen. In erfindungswesentlicher Weise wird das bei der Synthesegasverflüssigung entstehende Abgas 4, wie Kohlenmonoxid, Wasserstoff, Methan und höhere Kohlenwasserstoffe nun zusammen mit Methan über einen zusätzlichen Kreislauf zunächst in einen der Synthesegasumsetzungsvorrichtung 8 nachgeschalteten Reformer 9, der in der in Fig. 1 dargestellten Ausführungsform als autothermer Reformer vorliegt, geleitet, um dann in ein reines Synthesegas 5 konvertiert zu werden. Das reine Synthesegas 5 wird wiederum dem in die Synthesegasumsetzungsvorrichtung 8 geführten Hauptsynthesegasstrom 3 zugeführt. In the synthesis gas conversion apparatus 8, the synthesis gas liquefaction is carried out in a conventional manner, for example on the basis of Fischer-Tropsch synthesis or methanol synthesis, to produce the end product 10. In an embodiment essential to the invention, the resulting in the synthesis gas liquefaction 4, such as carbon monoxide, hydrogen, methane and higher hydrocarbons now together with methane via an additional circuit first in one of the synthesis gas conversion device 8 downstream reformer 9, in the embodiment shown in Fig. 1 as autothermal Reformer present, then passed to be converted into a pure synthesis gas 5. The pure synthesis gas 5 is in turn fed to the main synthesis gas stream 3 guided into the synthesis gas conversion device 8.
Natürlich ist die beschriebene Ausführungsform der Erfindung noch in vielfacher Hinsicht abzuändern, ohne den Grundgedanken der Erfindung zu verlassen. Bei¬ spielsweise können auch noch andere Vergasungstechniken als die Flugstrom- oder Wirbelschichtvergasung in dem Reaktor 6 zugrundegelegt werden. Auch können andere Technologien als Filterung und chemische Reaktionen für die Reinigung in der Reinigungsvorrichtung 7 angewendet werden. Auch kann der zusätzlich geschaltete Kreislauf mehrmals durchlaufen werden. Of course, the described embodiment of the invention is still to be modified in many ways, without departing from the spirit of the invention. In ¬ example, other gasification techniques than the flow stream or fluidized bed gasification in the reactor 6 can be used. Also, other technologies than filtering and chemical reactions for cleaning may be used in the cleaning device 7. Also, the additional circuit can be run through several times.
Bezuqszeichenliste: LIST OF REFERENCES:
1 Brennstoff 1 fuel
2 Synthesegas  2 synthesis gas
3 Synthesegasstrom  3 synthesis gas stream
4 Abgas  4 exhaust
5 Synthesegas  5 synthesis gas
6 Reaktor  6 reactor
7 Synthesereinigungsvorrichtung 7 Synthesizing device
8 Synthesegasumsetzungsvorrichtung8 synthesis gas conversion device
9 Reformer 9 reformers
10 Endprodukt  10 final product

Claims

Patentansprüche: claims:
1. Verfahren zur Herstellung von Synthesegas für die Umsetzung zu anderen Produkten, insbesondere für die Synthesegasverflüssigung mit folgenden Verfahrensschritten : 1. A process for the production of synthesis gas for the conversion to other products, in particular for the syngas liquefaction with the following process steps:
a) Zuführung eines kohlenstoffhaltigen Brennstoffes (1) in einen Reaktor (6), in dem der Brennstoff (1) mit Luft oder Sauerstoff oder sauerstoffangereicherter Luft sowie mit Wasserdampf und C02 bei erhöhter Temperatur, vorzugsweise bei Temperaturen von 800 - 1200° C oder höher, zu einem rohen Synthesegas (2) umgesetzt wird, das zu einem wesentlichen Teil aus Wasserstoff, Kohlendioxid und Kohlenmonoxid besteht und zusätzlich Anteile von Methan aufweist, b) Reinigung des rohen Synthesegases (2), wobei das gereinigte rohe Synthesegas (2) mit entstandenem Methan als Hauptsynthesegasstrom (3) der Synthesegasumsetzung zugeführt wird, bei der auch ein Abgas (4) produziert wird; a) supplying a carbonaceous fuel (1) into a reactor (6), in which the fuel (1) with air or oxygen or oxygen-enriched air and with water vapor and C0 2 at elevated temperature, preferably at temperatures of 800 - 1200 ° C or is converted to a crude synthesis gas (2), which consists essentially of hydrogen, carbon dioxide and carbon monoxide and additionally comprises proportions of methane, b) purification of the crude synthesis gas (2), wherein the purified crude synthesis gas (2) resulting methane as the main synthesis gas stream (3) of the synthesis gas conversion is supplied, in which also an exhaust gas (4) is produced;
c) Konvertierung des produzierten Abgases (4) in ein reines Synthesegas (5) und Zuführung des reinen Synthesegases (5) in den Hauptsynthesegasstrom (3). c) converting the exhaust gas produced (4) into a pure synthesis gas (5) and feeding the pure synthesis gas (5) into the main synthesis gas stream (3).
2. Verfahren nach Anspruch 1, 2. The method according to claim 1,
dadurch gekennzeichnet, characterized,
dass das Abgas (4) einem Reformer (9) zugeführt wird. that the exhaust gas (4) is fed to a reformer (9).
3. Verfahren nach Anspruch 2, 3. The method according to claim 2,
dadurch gekennzeichnet, characterized,
dass der Reformer (9) ein autothermer Reformer oder ein katalytischer Reformer ist. that the reformer (9) is an autothermal reformer or a catalytic reformer.
4. Verfahren nach Anspruch 2 oder 3, 4. The method according to claim 2 or 3,
dadurch gekennzeichnet, characterized,
dass der Reformer (9) einer Synthesegasumsetzungsvorrichtung (8) nachgeschaltet ist. in that the reformer (9) is connected downstream of a synthesis gas conversion device (8).
5. Verfahren nach Anspruch 4, 5. The method according to claim 4,
dadurch gekennzeichnet, characterized,
dass die Vorrichtung (8) zwischen einer Synthesegasreinigungsvorrichtung (7) und dem Reformer (9) angeordnet ist. in that the device (8) is arranged between a synthesis gas purification device (7) and the reformer (9).
6. Verfahren nach Ansprüche 4 oder 5, 6. The method according to claims 4 or 5,
dadurch gekennzeichnet, characterized,
dass die Vorrichtung (8) der Synthesegasreinigungsvorrichtung (7) nachgeschaltet ist. that the device (8) of the synthesis gas purification device (7) is connected downstream.
7. Verfahren nach einem der vorangehenden Ansprüche, 7. The method according to any one of the preceding claims,
dadurch gekennzeichnet, characterized,
dass Verfahrensschritt c) mehr als einmal durchgeführt wird. that process step c) is carried out more than once.
EP14714167.5A 2013-04-04 2014-03-25 Method for producing synthesis gas for conversion to products Withdrawn EP2981596A1 (en)

Applications Claiming Priority (2)

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DE102013103356.3A DE102013103356A1 (en) 2013-04-04 2013-04-04 Process for the production of synthesis gas for conversion to products
PCT/EP2014/000799 WO2014161640A1 (en) 2013-04-04 2014-03-25 Method for producing synthesis gas for conversion to products

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EP2981596A1 true EP2981596A1 (en) 2016-02-10

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CN (1) CN105247017A (en)
BR (1) BR112015025226A2 (en)
DE (1) DE102013103356A1 (en)
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WO (1) WO2014161640A1 (en)

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EP4086328A1 (en) 2021-05-06 2022-11-09 GIDARA Energy B.V. Method and apparatus for industrial production of renewable synthetic fuels

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US3972958A (en) * 1975-04-08 1976-08-03 Mobil Oil Corporation Conversion of coal to high octane gasoline
NZ587840A (en) * 2008-03-12 2012-02-24 Sasol Tech Pty Ltd Hydrocarbon synthesis
CA2954374A1 (en) * 2009-01-21 2010-08-12 Res Usa, Llc System and method for dual fluidized bed gasification
FI20115038L (en) * 2011-01-14 2012-07-15 Vapo Oy METHOD FOR UTILIZING THE HEAT ENERGY CONTAINED IN THE GASES FORMED IN THE BTL PLANT

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CN105247017A (en) 2016-01-13
DE102013103356A1 (en) 2014-10-09
BR112015025226A2 (en) 2017-07-18
WO2014161640A1 (en) 2014-10-09
WO2014161640A8 (en) 2015-10-22

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