WO2013088049A1 - Procédé pour une production de gaz de synthèse avec conservation du transfert d'énergie par les fumées - Google Patents
Procédé pour une production de gaz de synthèse avec conservation du transfert d'énergie par les fumées Download PDFInfo
- Publication number
- WO2013088049A1 WO2013088049A1 PCT/FR2012/052867 FR2012052867W WO2013088049A1 WO 2013088049 A1 WO2013088049 A1 WO 2013088049A1 FR 2012052867 W FR2012052867 W FR 2012052867W WO 2013088049 A1 WO2013088049 A1 WO 2013088049A1
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- WIPO (PCT)
- Prior art keywords
- air
- combustion
- fumes
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- gas
- Prior art date
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Classifications
-
- 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
- C01B3/38—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 using catalysts
- C01B3/384—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 using catalysts the catalyst being continuously externally heated
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
- C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
- C01B2203/0233—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a steam reforming step
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/042—Purification by adsorption on solids
- C01B2203/043—Regenerative adsorption process in two or more beds, one for adsorption, the other for regeneration
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/08—Methods of heating or cooling
- C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
- C01B2203/0811—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel
- C01B2203/0827—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel at least part of the fuel being a recycle stream
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/12—Feeding the process for making hydrogen or synthesis gas
- C01B2203/1205—Composition of the feed
- C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
- C01B2203/1235—Hydrocarbons
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/16—Controlling the process
- C01B2203/1695—Adjusting the feed of the combustion
-
- 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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Definitions
- the present invention relates to a process for producing synthesis gas from a hydrocarbon feedstock comprising at least one step of generating a raw synthesis gas by steam reforming with production of the heat necessary for reforming by combustion in a reforming furnace comprising a combustion chamber and a convection chamber for exhausting fumes, the combustion chamber containing vertical tubes filled with catalyst, able to circulate from top to bottom a mixture of hydrocarbons and water vapor, and burners supplied with fuel and oxidant, and producing by combustion flames capable of bringing to you the heat required for reforming, as well as stages of use of the heat contained in the fumes for the preheating and / or heating of different fluids linked or not to the process.
- H 2 / CO synthesis gas The generation of an H 2 / CO synthesis gas is done - among other things - by reforming methane or other light steam hydrocarbon fillers (steam methane reforming in English or SMR), and this at very high temperature. Several reactions occur during this reforming stage, and if some are exothermic, the initial and main reaction is endothermic, so that it is necessary to provide heat for this synthesis gas generation step. (or syngas).
- Different fuels are usually burned to provide this heat for reforming, among which a so-called primary fuel - typically a mixture of light hydrocarbons ranging from natural gas to naphtha, frequently a fraction taken from the feed gas - and that a so-called secondary fuel, constituted at least by one or more waste gases resulting directly or indirectly from the process of treatment of the synthesis gas produced, in particular in the case of a final production of hydrogen from of the synthesis gas produced, the secondary fuel will contain all or part of the waste gas (or offgas) of the hydrogen purification unit, usually a pressure modulation adsorption unit (PSA).
- PSA pressure modulation adsorption unit
- the required temperature levels in the reforming zone are very high, and since the temperature at which the reforming occurs is greater than 800 ° C (and in general greater than 850 ° C), a significant amount (typically between 40 to 60%) of the heat released during combustion is not used for reforming. In fact, only the part of heat released during combustion and having a temperature sufficient to bring heat to the reforming process is useful for the reaction. The rest of the heat released by the combustion must be valorized in the overall process to obtain an acceptable global thermal efficiency. This fraction of the heat of the combustion not used by the reforming reaction is found in the fumes from the reforming zone ( radiation) and is recovered in the convection zone. This heat recovery is carried out from temperature levels up to 1080 ° C to a lower temperature limit corresponding to the temperature below which the flue gas is admitted to the atmosphere (from order of 180 ° C or less depending on the standards in force).
- the heat available in the fumes can thus cover various needs, in particular: the preheating of the hydrocarbon feedstock;
- Steam generation is understood to mean - by extension - the heating of liquid water or water, as well as the demineralized water (DMW) and water of water. so-called boiler process (boiling feed water or BFW), vaporization and overheating of steam;
- preheating combustion air or process air exported.
- the different preheating takes place via exchangers present in the convection zone where the flue gas circulates.
- the fumes having been cooled during the different preheating are then emitted into the atmosphere via a blower and / or a chimney.
- the amount of heat available for these different heaters is a function of the temperature of the fumes, but also of course their flow.
- oxidants also known as oxidants
- oxygen supply oxygen supply
- the air can be oxygen-depleted air (but at least 10% 0 2 in air), or enriched with oxygen (up to 40% 0 2 in air).
- the air must always be in excess - relative to the stoichiometry of the combustion reaction - so that all combustible gases are consumed, but in limited excess. It is thus sought to adapt the amount of air, so as to keep the excess air at a level of at least 5%, without exceeding 40% relative to the needs of the stoichiometry of combustion, preferably between 5% and 20% compared to stoichiometry. Ensuring limited excess air allows:
- the inert compounds extracted from the secondary fuel did not contribute to the fuel, their presence nevertheless required additional fuel to heat them up to the temperature level necessary for a flame temperature allowing the reforming reaction to place with proper efficiency.
- Their presence in the fumes contributed to the volume of these fumes and represented a large amount of heat that could be used in the convection zone; a reduction in the amount of inert compounds in the gas mixture sent to the burners therefore means reduced heating requirements, a decreased fuel requirement, and therefore a need for oxidizer, ie air also decreased.
- maintaining the excess air within the limits required for the oxygen content in the flue gases to remain below the MOC also contributes to the reduction of the total mass flow of fumes.
- a first consequence of the reduction of the flue gas volume is that the primary function of the combustion being to meet the needs of the reforming reaction, the reduction of the heat input to the tubes by the combustion gases emitted in the chamber. Combustion will be compensated by an appropriate increase in the oxidant (air) feed and by a larger addition of primary fuel.
- a first problem resides in the fact that it is no longer possible to maintain the preheating temperatures and / or the quantities of fluids preheated in the convection zone as they were ensured when the inerts were present in the fumes. This reduction of the possibilities of preheating via the fumes can be detrimental for the reforming process itself (reduction of the reforming efficiency due to insufficient preheating of the various reagents, reduction of the steam production).
- a second problem then arises, the exchangers present in the convection zone being designed with determined operating ranges, depending on the quantity of the inert compounds removed, it may be outside the appropriate ranges which will require expensive modifications of the latter. .
- the object of the invention is to propose a reforming process in a steam reforming furnace which, in the event of a decrease in the flow of fuel gas secondary reaction resulting from a modification of the composition of the gas mixture supplying the secondary fuel, either by reducing the content of inert compounds or by reducing the content of all or part of the compounds participating in the combustion reaction with air (typically CO, CH 4 , H 2 ) in said fuel gas, to maintain transferable heat from the convection zone by maintaining the flue gas flow in the convection zone.
- air typically CO, CH 4 , H 2
- the invention thus relates to a process for producing synthesis gas - intended for a final production of hydrogen -, from a hydrocarbon feedstock comprising at least:
- a step of generating a raw synthesis gas by steam reforming said hydrocarbon feedstock with production of the heat necessary for reforming by means of a combustion, said step of generating the synthesis gas being carried out in a reforming furnace comprising at least:
- a combustion chamber containing one or more rows of vertical tubes filled with catalyst, able to circulate up and down a mixture containing the hydrocarbon feedstock and water vapor, so as to recover the tubes down the raw synthesis gas, and burners arranged in rows, said burners being supplied with fuel and combustion air and producing by combustion flames able to heat the tubes and gases; at least one convection chamber able to evacuate fumes containing the gases produced by the combustion,
- the fuel comprises at least one primary fuel and a secondary fuel, which itself comprises at least one waste gas in connection with the synthesis gas production process
- the reduction of the mass flow of fumes comes mainly from the modification of the composition of the secondary fuel.
- the method is thus particularly advantageous when the synthesis gas undergoes separation of the hydrogen contained by pressure swing adsorption (PSA) to produce hydrogen and the secondary fuel used contains waste gas from said separation, in particular, in the case where the reduction of the mass flow of the fumes is due to the fact that carbon dioxide has been removed from the waste gas in connection with the hydrogen production process prior to its use as a secondary fuel; but also in the case where at least a part of the reduction of the fumes comes from the fact that carbon monoxide and / or methane and / or hydrogen has been removed from the waste gas in relation to the production process of hydrogen prior to its use as a secondary fuel.
- PSA pressure swing adsorption
- the invention makes it possible to maintain the capacity of the fumes to ensure the required preheating and heating of fluids, and also makes it possible to operate the various exchangers and other related materials satisfactorily.
- the invention may have all or some of the following features:
- the additional gas flow rate supplied to the combustion zone is a flow rate of gas that is inert with respect to the combustion reaction
- this inert gas can be nitrogen
- a nitrogen flow rate can be injected into the combustion air, via one or more injections upstream of the 1st air preheating exchanger, or downstream of said 1st air preheating exchanger, and in case of presence a second air preheating exchanger, upstream or downstream of said 2 nd air preheating exchanger; the additional inert gas flow supplied to the combustion zone may be saturated or superheated water vapor;
- the water vapor can directly feed the burners of the combustion zone, independently of the combustion air and the fuel;
- the water vapor can alternatively be premixed with the combustion air, or with the fuel;
- the water vapor can come from the reforming process itself or be imported.
- the steam if the steam is available at an excessive pressure, it can be previously relaxed to a pressure compatible with its use, generally at low pressure, preferably less than 5 bara;
- the fuel flow rate (primary and / or secondary) can be adapted to take into account the modification of the gas composition at the level of combustion related to the introduction of an inert gas different from that to which it is substituted;
- the additional gas flow brought into the combustion zone may be an additional air flow rate when the excess air before addition of the additional gas flow is low, between 5% and 20%; in this case, the additional gas flow supplied to the combustion zone may be a flow of air, provided that the additional supply is made so that the excess air remains below 40%;
- the injection of the additional air flow can be achieved via the existing fresh air blower and / or a new air blower, either of sufficient capacity to replace the existing fresh air blower, or additional blower, and intended for the total or partial treatment of the additional air flow in addition to the existing fresh air blower;
- the portion of the additional air flow through the new additional blower is injected into the combustion air, either upstream du1 first air preheating exchanger or downstream of said 1st air preheat exchanger and in case of presence of a 2nd air preheat exchanger, upstream or downstream of said 2nd air.
- - preheat exchanger advantageously, add a device for monitoring the hydrocarbon content in the flue gas, which can be coupled to a reformer safety device (reforming stop, air flow reduction, etc.) so as to detect the presence of hydrocarbons in the flue gases.
- this device therefore allows to accept a higher oxygen content in the fumes without risk.
- This improvement is particularly useful, in the context of the invention, when one chooses to increase the air content in the fumes; more generally, this device is useful when the oxygen content in the fumes is close to the MOC, it may indeed be that in certain particular circumstances, this acceptable upper limit of 0 2 concentration is reached or exceeded, for example during operation of the facility in degraded operation that it is a reduced capacity operation, or during transient phases, or other, and that the excess oxygen leads to an oxygen concentration higher than the MOC.
- the addition of this device allows the operation of the reformer thus protected in case of reduced capacity running, starting, stopping, increasing or decreasing the capacity.
- This improvement can be planned during the construction of the installation, or be part of a modification of the installation.
- FIG. 1 is a schematic view of a steam reforming furnace known , heated by the top (top fired);
- Figure 2 is a schematic view of a steam reforming furnace heated from above, adapted to implement a variant of the method according to the invention
- Figure 3 is a schematic view of a steam reforming furnace heated from above, suitable for the implementation of a second variant of the method of the invention
- FIG. 4 is a schematic view of a top-heated steam reforming furnace suitable for implementing a third variant of the process according to the invention.
- Figure 1 shows a schematic view of a known top-heated steam reforming furnace, showing the various constituent elements of the reformer useful for understanding the invention, as well as the various fluids circulating.
- the treatment of the synthesis gas 8, downstream of the reformer to obtain hydrogen is not shown. Typically, it is a treatment with PSA, with production of a waste gas.
- combustion chamber 1 the convection chamber 2.
- the combustion chamber is equipped with burners in the vault 3, supplied with 4 fuel: fuel 4A and residual PSA 4B, and preheated air as the oxidant 5.
- the feed gas of the preheated process 6 feeds the reforming tubes 7.
- the synthesis gas 8 is recovered at the outlet of the reforming tubes.
- the preheated air is obtained from fresh air, injected via a fresh combustion air blower 9, and preheated here in air preheaters 10 and then optionally at 12.
- the evacuation of the combustion gases thus cooled is carried out via a fan 19 for extracting the fumes.
- FIG. 2 shows a schematic view of a top fired steam reforming furnace, suitable for the implementation of a first variant of the invention.
- This oven differs from that of FIG. 1 in that it is furthermore equipped with means for supplying an additional combustion air flow, said means comprising a source 16 of additional fresh air, an additional fan 17 , intended to treat all or part of the additional fresh air flow - it should be noted that if the capacity of the blower 9 is sufficient to receive the total fresh air flow, it will not be necessary to add this second blower 16, it is also possible to replace the existing fan 9 with a new fan 9, of sufficient capacity to treat all the combustion air.
- the blown additional air 18 can be injected in whole or in part at 18A upstream of the preheater 1 0, or downstream of the air preheater 10, in this second case, it can be injected at 18B upstream or 18C downstream of the optional air preheater 12.
- the oven according to the invention as presented here also has a device 20 for monitoring the hydrocarbon content of the fumes; this monitoring device 20 is coupled to a device for making the reformer safe (not shown in the figure) which allows in case of detection of hydrocarbons - which hydrocarbons could come from a leak in the means of preheating 14 and / or 1 5 - to modify the running of the installation, or to stop it in according to the defined security protocol.
- This protocol can provide for example a reduction of the air flow, a stop reformer, or any other appropriate solution.
- FIG 3 shows a schematic view of a steam reforming furnace heated by the top (fired), suitable for the implementation of a second embodiment of the invention.
- This oven differs from that of Figure 1 in that it is further equipped with means for feeding a flow 21 of nitrogen (or more generally of inert gas) in addition to the flow of combustion air.
- the injection of inert gas can be done, in the same way as that of additional air, that is to say wholly or partly at 22A upstream of the preheater 10, or downstream of the air preheater 10 in this second case, it can be injected at 22B upstream, or at 22C downstream, of the optional air preheater 12.
- This injection of inert gas is intended to compensate for the reduction - in the flue gas - of inerts (essentially C0 2 ) normally present in the waste (offgas) of PSA supplying the burners.
- FIG. 4 shows a schematic view of a top fired steam reforming furnace, suitable for the implementation of a third variant of the invention.
- This oven differs from that of FIG. 1 in that it is furthermore equipped with steam injection means 23 (saturated or superheated) replacing the inert gases that were taken before or after the PSA (C0 2 essentially, but also potentially nitrogen and other inerts).
- the steam may be injected in whole or in part at 24A into the preheated combustion air, or wholly or partly at 24B in the fuel oil. It can also - according to a mode not shown in the figure - be injected into each of the burners separately from the combustion air and fuel oil.
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Health & Medical Sciences (AREA)
- General Health & Medical Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Inorganic Chemistry (AREA)
- Hydrogen, Water And Hydrids (AREA)
Abstract
Description
Claims
Priority Applications (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CA2856239A CA2856239A1 (fr) | 2011-12-14 | 2012-12-11 | Procede pour une production de gaz de synthese avec conservation du transfert d'energie par les fumees |
JP2014546610A JP2015501780A (ja) | 2011-12-14 | 2012-12-11 | ヒューム(fumes)によるエネルギー伝達の保存を伴う合成ガスを生産するための方法 |
US14/364,307 US9321643B2 (en) | 2011-12-14 | 2012-12-11 | Process for producing synthesis gas with preservation of the energy transfer by means of the fumes |
EP12810383.5A EP2791051A1 (fr) | 2011-12-14 | 2012-12-11 | Procédé pour une production de gaz de synthèse avec conservation du transfert d'énergie par les fumées |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR1161591 | 2011-12-14 | ||
FR1161591A FR2984297B1 (fr) | 2011-12-14 | 2011-12-14 | Procede pour une production de gaz de synthese avec conservation du transfert d'energie par les fumees |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2013088049A1 true WO2013088049A1 (fr) | 2013-06-20 |
Family
ID=47505245
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/FR2012/052867 WO2013088049A1 (fr) | 2011-12-14 | 2012-12-11 | Procédé pour une production de gaz de synthèse avec conservation du transfert d'énergie par les fumées |
Country Status (6)
Country | Link |
---|---|
US (1) | US9321643B2 (fr) |
EP (1) | EP2791051A1 (fr) |
JP (1) | JP2015501780A (fr) |
CA (1) | CA2856239A1 (fr) |
FR (1) | FR2984297B1 (fr) |
WO (1) | WO2013088049A1 (fr) |
Families Citing this family (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN110121586B (zh) | 2016-11-09 | 2022-01-25 | 八河流资产有限责任公司 | 用于电力生产和集成的氢气生产的系统和方法 |
WO2020250194A1 (fr) | 2019-06-13 | 2020-12-17 | 8 Rivers Capital, Llc | Production d'énergie cogénérant d'autres produits |
WO2023089570A1 (fr) | 2021-11-18 | 2023-05-25 | 8 Rivers Capital, Llc | Appareil de production d'hydrogène |
Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US20030110693A1 (en) * | 2001-12-17 | 2003-06-19 | Drnevich Raymond Francis | Production enhancement for a reactor |
US20070104641A1 (en) * | 2005-11-08 | 2007-05-10 | Ahmed M M | Method of controlling oxygen addition to a steam methane reformer |
US20090298957A1 (en) * | 2004-11-16 | 2009-12-03 | Pierre-Robert Gauthier | Method and installation for combined production of hydrogen and carbon dioxide |
US20100255432A1 (en) * | 2007-07-12 | 2010-10-07 | L'air Liquide Societe Anonyme Pour L'etude Et L'ex Ploitation Des Procedes Georges Claude | Method Of Regulating The Flow Of Combustible Gas During The Start-Up Phase Of A Reforming Furnace |
Family Cites Families (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE102010020406B4 (de) * | 2009-12-16 | 2012-02-09 | Lurgi Gmbh | Verfahren zum Betreiben eines Reformerofens und Reformeranlage |
-
2011
- 2011-12-14 FR FR1161591A patent/FR2984297B1/fr active Active
-
2012
- 2012-12-11 WO PCT/FR2012/052867 patent/WO2013088049A1/fr active Application Filing
- 2012-12-11 US US14/364,307 patent/US9321643B2/en active Active
- 2012-12-11 JP JP2014546610A patent/JP2015501780A/ja active Pending
- 2012-12-11 EP EP12810383.5A patent/EP2791051A1/fr not_active Withdrawn
- 2012-12-11 CA CA2856239A patent/CA2856239A1/fr not_active Abandoned
Patent Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US20030110693A1 (en) * | 2001-12-17 | 2003-06-19 | Drnevich Raymond Francis | Production enhancement for a reactor |
US20090298957A1 (en) * | 2004-11-16 | 2009-12-03 | Pierre-Robert Gauthier | Method and installation for combined production of hydrogen and carbon dioxide |
US20070104641A1 (en) * | 2005-11-08 | 2007-05-10 | Ahmed M M | Method of controlling oxygen addition to a steam methane reformer |
US20100255432A1 (en) * | 2007-07-12 | 2010-10-07 | L'air Liquide Societe Anonyme Pour L'etude Et L'ex Ploitation Des Procedes Georges Claude | Method Of Regulating The Flow Of Combustible Gas During The Start-Up Phase Of A Reforming Furnace |
Also Published As
Publication number | Publication date |
---|---|
US20140374662A1 (en) | 2014-12-25 |
EP2791051A1 (fr) | 2014-10-22 |
FR2984297B1 (fr) | 2014-08-08 |
FR2984297A1 (fr) | 2013-06-21 |
CA2856239A1 (fr) | 2013-06-20 |
US9321643B2 (en) | 2016-04-26 |
JP2015501780A (ja) | 2015-01-19 |
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