DE3602352A1 - Process for isolating hydrogen - Google Patents

Process for isolating hydrogen

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Publication number
DE3602352A1
DE3602352A1 DE19863602352 DE3602352A DE3602352A1 DE 3602352 A1 DE3602352 A1 DE 3602352A1 DE 19863602352 DE19863602352 DE 19863602352 DE 3602352 A DE3602352 A DE 3602352A DE 3602352 A1 DE3602352 A1 DE 3602352A1
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DE
Germany
Prior art keywords
hydrogen
pressure swing
swing adsorption
gas
conversion
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Withdrawn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
DE19863602352
Other languages
German (de)
Inventor
Allan Dr Watson
Bernd Dipl Ing Kandziora
Christian Dipl Ing Benkmann
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.)
Linde GmbH
Original Assignee
Linde GmbH
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 Linde GmbH filed Critical Linde GmbH
Priority to DE19863602352 priority Critical patent/DE3602352A1/en
Publication of DE3602352A1 publication Critical patent/DE3602352A1/en
Withdrawn legal-status Critical Current

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/48—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents followed by reaction of water vapour with carbon monoxide
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
    • C01B3/56—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2256/00—Main component in the product gas stream after treatment
    • B01D2256/16—Hydrogen
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/40001—Methods relating to additional, e.g. intermediate, treatment of process gas
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/402—Further details for adsorption processes and devices using two beds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/404—Further details for adsorption processes and devices using four beds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/047—Pressure swing adsorption

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Inorganic Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Analytical Chemistry (AREA)
  • Separation Of Gases By Adsorption (AREA)
  • Hydrogen, Water And Hydrids (AREA)

Abstract

A process is proposed for isolating hydrogen by catalytic reforming of hydrocarbons with subsequent conversion of the synthesis gases thus formed and subsequently separating off the hydrogen by means of a pressure-change adsorption process. The residual gas obtained in the pressure-change adsorption is compressed and at least in part recirculated to the reforming or conversion and at least in part fed to a further pressure-change adsorption.

Description

Die Erfindung betrifft ein Verfahren zur Gewinnung von Wasserstoff durch katalytische Reformierung von Kohlen­ wasserstoffen, Konvertierung der dabei gebildeten Synthesegase und nachfolgender Abtrennung von Wasserstoff mittels eines Druckwechseladsorptionsverfahrens.The invention relates to a method for obtaining Hydrogen through catalytic reforming of coal hydrogen, conversion of the formed Synthesis gases and subsequent separation of hydrogen by means of a pressure swing adsorption process.

Bei der Gewinnung von Wasserstoff aus leichten Kohlen­ wasserstoffen wie Erdgas, LPG oder Benzinfraktionen wird ein solches Verfahren häufig großtechnisch eingesetzt.When extracting hydrogen from light coal Hydrogen such as natural gas, LPG or gasoline fractions such a process is often used on an industrial scale.

Der Erfindung liegt die Aufgabe zugrunde, ein derartiges Verfahren so auszugestalten, daß bei möglichst geringen Investitionskosten eine hohe Wasserstoffausbeute erzielt werden kann.The invention has for its object such To design the process so that the lowest possible Investment costs achieved a high hydrogen yield can be.

Diese Aufgabe wird dadurch gelöst, daß das bei der Druck­ wechseladsorption anfallende Restgas verdichtet und mindestens teilweise in die Reformierung oder Konvertierung zurückgeführt und mindestens teilweise einer weiteren Druckwechseladsorption zugeführt wird. This object is achieved in that the pressure alternating adsorption resulting residual gas compressed and at least partially in reforming or converting returned and at least partially another Pressure swing adsorption is supplied.  

In einer ersten Ausgestaltung der Erfindung kann das Rest­ gas der Druckwechseladsorption in zwei Teilströme aufge­ teilt werden, wobei der erste Teilstrom in die Reformierung bzw. Konvertierung zurückgeführt wird, während der zweite Teilstrom der weiteren Druckwechseladsorptionsanlage zugeleitet wird. Der zweite Teilstrom sollte dabei so groß sein, daß Inertbestandteile des Synthesegases über das Restgas der weiteren Druckwechseladsorptionsanlage so weit ausgetragen werden, daß keine Anreicherung dieser Komponenten in der Anlage erfolgt.In a first embodiment of the invention, the rest Gas the pressure swing adsorption in two partial flows be divided, the first partial flow into the reforming or conversion is returned while the second Partial flow of the further pressure swing adsorption system is forwarded. The second partial flow should be like this be great that inert components of the synthesis gas over the residual gas from the further pressure swing adsorption system are carried out so far that no enrichment of this Components in the system.

In einer anderen Ausgestaltung der Erfindung ist vorge­ sehen, daß der rückgeführte Teilstrom nach seiner Um­ wandlung in der Reformierung und/oder Konvertierung der weiteren Druckwechseladsorptionsanlage zugeführt wird.In another embodiment of the invention is provided see that the recirculated partial flow after its order change in reforming and / or converting the another pressure swing adsorption system is supplied.

Ein wesentlicher Vorteil des erfindungsgemäßen Verfahrens ist darin zu sehen, daß aus dem Spülgas der Druckwechsel­ adsorptionsanlage noch zusätzlicher Wasserstoff gewonnen wird, was entweder direkt durch Zuführung des Spülgases in eine weitere Adsorptionsanlage erfolgt oder nach Umwandlung der im Spülgas noch enthaltenen Kohlenwasser­ stoffe und/oder Kohlenmonoxid zu Wasserstoff.A major advantage of the method according to the invention can be seen in the fact that the pressure change from the purge gas adsorption system won additional hydrogen becomes what is either directly by supplying the purge gas into another adsorption plant or after Conversion of the hydrocarbon still contained in the purge gas substances and / or carbon monoxide to hydrogen.

Gegenüber einem üblichen Verfahren der eingangs genannten Art fällt beim erfindungsgemäßen Verfahren ein relativ kleiner abzuführender Spülgasstrom aus der zweiten Druckwechseladsorptionsanlage an. Eine übliche Verwendung des Spülgases besteht darin, den Reformer zu beheizen. Dies ist jedoch oftmals ungünstig, weil dadurch ein Teil des durch die Anlage geführten Gases letztendlich nur zu Heizzwecken verwendet wird. Dies trifft insbeson­ dere dann zu, wenn preisgünstige andere Heizgase zur Verfügung stehen. Bei einer üblichen Wasserstoffausbeute von etwa 80% bei der Druckwechseladsorption werden somit etwa 20% des gebildeten Wasserstoffs nur zu Heizzwecken verwendet.Across from a usual method of the type mentioned falls relatively in the inventive method small purge gas flow to be removed from the second Pressure swing adsorption system. A common use of the purge gas is to heat the reformer. However, this is often inconvenient because of this Part of the gas passed through the plant ultimately is only used for heating purposes. This is particularly true then when low-cost other heating gases are used To be available. With a normal hydrogen yield of about 80% in pressure swing adsorption thus only about 20% of the hydrogen formed  Used for heating purposes.

Bei Durchführung des erfindungsge­ mäßen Verfahrens läßt sich dieser Wasserstoff sowie gegebenenfalls zusätzlicher Wasserstoff bilden, womit die Gesamtausbeute beispielsweise von etwa 80 auf über 95% Wasserstoff ansteigt. Sofern eine bestimmte Menge Wasser­ stoff benötigt wird, bedeutet dies andererseits eine entsprechende Reduzierung der Anlagenteile.When performing the fiction This process can be hydrogen as well optionally form additional hydrogen, with which Overall yield, for example from about 80 to over 95% Hydrogen increases. Unless a certain amount of water on the other hand, this means a corresponding reduction of the system parts.

In beiden Druckwechseladsorptionsanlagen wird Wasserstoff als nicht adsorbierbare Komponente in reiner Form gewonnen. Es ist deshalb in vielen Fällen vorteilhaft, diese beiden Anlagen austrittsseitig zu koppeln, wie es in der DE-OS 30 46 267 beschrieben ist.Hydrogen is produced in both pressure swing adsorption plants obtained as a non-adsorbable component in pure form. It is therefore beneficial in many cases to use both of these Coupling systems on the outlet side, as in the DE-OS 30 46 267 is described.

Weitere Einzelheiten der Erfindung werden nachfolgend anhand der in den Figuren schematisch dargestellten Ausführungsbeispiele erläutert.Further details of the invention are set out below based on the schematically shown in the figures Exemplary embodiments explained.

Es zeigen:Show it:

Fig. 1 eine erste Ausführungsform der Erfindung und Fig. 1 shows a first embodiment of the invention and

Fig. 2 eine weitere Ausführungsform der Erfindung. Fig. 2 shows a further embodiment of the invention.

Bei dem in Fig. 1 dargestellten Ausführungsbeispiel wird über Leitung 1 ein Einsatzgas, beispielsweise Erdgas, LPG, Raffineriegase oder Benzinfraktionen nach Vermischung mit Wasserdampf einem Dampfreformierer 2 zugeführt. Durch die endotherme katalytische Reaktion wird ein im wesent­ lichen Wasserstoff, Oxide des Kohlenstoffs und zum Teil nicht umgesetzte Kohlenwasserstoffe sowie gegebenenfalls vorhandene Inertgasbestandteile enthaltendes Synthesegas erzeugt. Das Gas wird über Leitung 3 abgezogen und nach Vermischung mit einem über Leitung 4 herangeführten Rückführgas einer Hochtemperaturkonvertierung 5 zugeführt, um im Gas enthaltenes Kohlenmonoxid mit Wasserdampf zu Wasserstoff und Kohlendioxid umzusetzen. Das Gas gelangt dann über Leitung 6 in eine CO2-Wäsche 7 und anschließend über Leitung 8 in eine erste Druckwechseladsorptions­ anlage 9. Gereinigter Wasserstoff tritt über Leitung 10 aus und wird über die Produktleitung 11 abgeführt. Das bei der Adsorption anfallende Restgas gelangt über Leitung 12 zu einem Kompressor 13 und wird danach in zwei Teilströme aufgeteilt. Ein erster Teilstrom wird über Leitung 4 vor die Hochtemperaturkonvertierung 5 zurückgeführt und gemeinsam mit dem über Leitung 3 herangeführten Gas weiter verarbeitet, während der zweite Teilstrom über Leitung 14 einer zweiten Druckwechsel­ adsorptionsanlage 15 zugeführt wird. Im Restgas noch ent­ haltener Wasserstoff wird dabei abgetrennt und über Leitung 16 abgezogen, um schließlich gemeinsam mit dem über Leitung 10 abgezogenen Wasserstoff über Leitung 11 als Produkt abgeführt zu werden. Das Restgas der zweiten Druckwechseladsorptionsanlage 15 gelangt über Leitung 17 zunächst in den Regenerierteil der CO2-Wäsche 7, wo es als Strippgas eingesetzt wird und dann über Leitung 19 zum Dampfreformierer 2, um dort als Heizgas eingesetzt zu werden. Zusätzliches Heizgas wird über Leitung 20 zugeführt.In the exemplary embodiment shown in FIG. 1, a feed gas, for example natural gas, LPG, refinery gases or gasoline fractions after mixing with steam, is fed to a steam reformer 2 via line 1 . The endothermic catalytic reaction generates an essentially union hydrogen, oxides of carbon and partially unreacted hydrocarbons as well as synthesis gas containing any inert gas components. The gas is drawn off via line 3 and, after mixing with a return gas supplied via line 4 , is fed to a high-temperature conversion 5 in order to convert carbon monoxide contained in the gas with water vapor to hydrogen and carbon dioxide. The gas then passes via line 6 into a CO 2 scrubber 7 and then via line 8 into a first pressure swing adsorption system 9 . Purified hydrogen exits via line 10 and is discharged via product line 11 . The residual gas resulting from the adsorption passes via line 12 to a compressor 13 and is then divided into two partial flows. A first partial stream is returned via line 4 before the high-temperature conversion 5 and further processed together with the gas brought in via line 3 , while the second partial stream is fed via line 14 to a second pressure swing adsorption system 15 . Hydrogen still contained in the residual gas is separated off and drawn off via line 16 , in order to finally be discharged as a product via line 11 together with the hydrogen drawn off via line 10 . The residual gas of the second pressure swing adsorption system 15 first reaches the regeneration part of the CO 2 scrubber 7 via line 17 , where it is used as stripping gas and then via line 19 to the steam reformer 2 , in order to be used there as heating gas. Additional heating gas is supplied via line 20 .

Das in der Fig. 2 dargestellte Ausführungsbeispiel unterscheidet sich von demjenigen der Fig. 1 dadurch, daß das Restgas 12 der ersten Druckwechseladsorptionsanlage nach der Verdichtung über Leitung 21 zum Dampfreformer zurückgeführt wird. Für die Umsetzung dieses Gases sind im Reformer 1 einige zusätzliche Rohre 1 a vorgesehen. Das reformierte Gas tritt über Leitung 3 a ebenfalls in die Hochtemperaturkonvertierung ein, wozu ein ge­ sonderter Querschnitt 5 a vorgesehen ist. Das umgewandelte Restgas gelangt dann über Leitung 22 in die zweite Druck­ wechseladsorptionsanlage 15.The exemplary embodiment shown in FIG. 2 differs from that of FIG. 1 in that the residual gas 12 of the first pressure swing adsorption system is returned to the steam reformer after compression via line 21 . For the implementation of this gas, a few additional tubes 1 a are provided in the reformer 1 . The reformed gas also enters via line 3 a in the high temperature conversion, for which purpose a special cross section 5 a is provided. The converted residual gas then passes via line 22 into the second pressure swing adsorption system 15 .

In einer alternativen Anordnung kann das über Leitung 21 abgezogene Restgas der ersten Druckwechselanlage auch direkt in die Hochtemperaturkonvertierung 5 a geleitet werden, was durch die gestrichelte Leitung 23 angedeutet ist.In an alternative arrangement, the residual gas drawn off via line 21 of the first pressure swing system can also be passed directly into the high-temperature conversion 5 a , which is indicated by the dashed line 23 .

Claims (4)

1. Verfahren zur Gewinnung von Wasserstoff durch katalyti­ sche Reformierung von Kohlenwasserstoffen, Konvertierung der dabei gebildeten Synthesegase und nachfolgender Abtrennung von Wasserstoff mittels eines Druckwechsel­ adsorptionsverfahrens, dadurch gekennzeichnet, daß das bei der Druckwechseladsorption anfallende Restgas verdichtet und mindestens teilweise in die Reformierung oder Konvertierung zurückgeführt und mindestens teilweise einer weiteren Druckwechseladsorption zuge­ führt wird.1. A process for the production of hydrogen by catalytic reforming of hydrocarbons, conversion of the synthesis gases formed and subsequent separation of hydrogen by means of a pressure swing adsorption process, characterized in that the residual gas obtained during the pressure swing adsorption compresses and at least partially recycled into the reforming or conversion and at least partially leads to a further pressure swing adsorption. 2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß ein nicht zurückgeführter Teilstrom der weiteren Druckwechseladsorption zugeführt wird.2. The method according to claim 1, characterized in that a non-recycled partial flow of the others Pressure swing adsorption is supplied. 3. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß der rückgeführte Teilstrom nach seiner Reformierung und/oder Konvertierung der weiteren Druckwechsel­ adsorption zugeführt wird. 3. The method according to claim 1, characterized in that the returned partial stream after its reforming and / or conversion of further pressure changes adsorption is supplied.   4. Verfahren nach einem der Ansprüche 1 bis 3, dadurch gekennzeichnet, daß die beiden Druckwechseladsorp­ tionsanlagen austrittsseitig gekoppelt sind.4. The method according to any one of claims 1 to 3, characterized characterized in that the two pressure swing adsorb tion systems are coupled on the outlet side.
DE19863602352 1986-01-27 1986-01-27 Process for isolating hydrogen Withdrawn DE3602352A1 (en)

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Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0259041A2 (en) * 1986-08-27 1988-03-09 Imperial Chemical Industries Plc Nitrogen production
DE3802555A1 (en) * 1988-01-28 1989-08-03 Linde Ag Process for operating a synthesis gas plant and plant for carrying out the process
DE10101098A1 (en) * 2001-01-12 2002-07-25 Emitec Emissionstechnologie Process for operating a reforming device comprises introducing a feed stream to a first reformer unit, removing a waste stream, deviating a partial stream from the waste stream and introducing to the feed stream to form a circulating stream
WO2005012166A1 (en) * 2003-07-28 2005-02-10 Uhde Gmbh Method for extracting hydrogen from a gas containing methane, especially natural gas and system for carrying out said method
FR2878763A1 (en) * 2004-12-07 2006-06-09 Air Liquide Process for improving hydrogen rich gas effluent in refineries comprises adjusting low hydrogen gas effluent to specific pressure, treating gas effluent, reinjecting part of enriched flow into catalytic reforming unit and removing hydrogen
DE102007054768A1 (en) * 2007-11-16 2009-05-20 J. Eberspächer GmbH & Co. KG Reformer, fuel cell and related operating procedures
WO2010018550A1 (en) * 2008-08-13 2010-02-18 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Novel steam reformer based hydrogen plant scheme for enhanced carbon dioxide recovery

Cited By (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0259041A2 (en) * 1986-08-27 1988-03-09 Imperial Chemical Industries Plc Nitrogen production
EP0259041A3 (en) * 1986-08-27 1990-05-23 Imperial Chemical Industries Plc Nitrogen production
DE3802555A1 (en) * 1988-01-28 1989-08-03 Linde Ag Process for operating a synthesis gas plant and plant for carrying out the process
DE10101098A1 (en) * 2001-01-12 2002-07-25 Emitec Emissionstechnologie Process for operating a reforming device comprises introducing a feed stream to a first reformer unit, removing a waste stream, deviating a partial stream from the waste stream and introducing to the feed stream to form a circulating stream
JP2007500115A (en) * 2003-07-28 2007-01-11 ウーデ・ゲゼルシャフト・ミト・ベシュレンクテル・ハフツング Process for producing hydrogen from methane-containing gas, in particular natural gas, and system for carrying out the process
WO2005012166A1 (en) * 2003-07-28 2005-02-10 Uhde Gmbh Method for extracting hydrogen from a gas containing methane, especially natural gas and system for carrying out said method
CN100347077C (en) * 2003-07-28 2007-11-07 犹德有限公司 Method for extracting hydrogen from a gas containing methane, especially natural gas and system for carrying out said method
US7682597B2 (en) 2003-07-28 2010-03-23 Uhde Gmbh Method for extracting hydrogen from a gas that contains methane, especially natural gas, and system for carrying out said method
JP4707665B2 (en) * 2003-07-28 2011-06-22 ウーデ・ゲゼルシャフト・ミト・ベシュレンクテル・ハフツング Process for producing hydrogen from methane-containing gas, in particular natural gas, and system for carrying out the process
NO337257B1 (en) * 2003-07-28 2016-02-29 Uhde Gmbh Process for extracting hydrogen from a methane-containing gas, in particular a natural gas, and plants for carrying out the process
FR2878763A1 (en) * 2004-12-07 2006-06-09 Air Liquide Process for improving hydrogen rich gas effluent in refineries comprises adjusting low hydrogen gas effluent to specific pressure, treating gas effluent, reinjecting part of enriched flow into catalytic reforming unit and removing hydrogen
DE102007054768A1 (en) * 2007-11-16 2009-05-20 J. Eberspächer GmbH & Co. KG Reformer, fuel cell and related operating procedures
WO2010018550A1 (en) * 2008-08-13 2010-02-18 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Novel steam reformer based hydrogen plant scheme for enhanced carbon dioxide recovery
US9481573B2 (en) 2008-08-13 2016-11-01 L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Steam reformer based hydrogen plant scheme for enhanced carbon dioxide recovery

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