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; Reversible storage of hydrogen
  • C01B3/02—Production of hydrogen; Production of gaseous mixtures containing hydrogen
  • C01B3/32—Production of hydrogen; Production of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide or air
  • C01B3/34—Production of hydrogen; Production of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide or air by reaction of hydrocarbons with gasifying agents
  • C01B3/38—Production of hydrogen; Production of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide or air by reaction of hydrocarbons with gasifying agents using catalysts
  • C01B3/384—Production of hydrogen; Production of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide or air by reaction of hydrocarbons with gasifying agents using catalysts with external heating of the catalyst

Definitions

• the present invention relates to a unit for the production and treatment of a synthesis gas obtained by reforming from a mixture of light hydrocarbons, of the type comprising at least one steam methane reformer (SMR) for the production of a synthesis gas, as well as elements
• SMR steam methane reformer
• the unit will conventionally comprise, in addition to the steam reformer, all or part of the following independent functional elements: a hydrodesulfurization module (hydro-desulfurization system or HDS in English), one or more elements functional cooling of the synthesis gas, a CO conversion module (English language shift), optionally a CO 2 removal module, a hydrogen separation module generally by pressure swing adsorption (pressure swing adsorption) or PSA in English), but also compressors as well as other various technical elements which are function of the supplies received from the outside - of the supplier or the customer - and made available in battery in limit.
• a hydrodesulfurization module hydro-desulfurization system or HDS in English
• one or more elements functional cooling of the synthesis gas a CO conversion module (English language shift)
• a CO conversion module English language shift
• optionally a CO 2 removal module optionally a CO 2 removal module
• a hydrogen separation module generally by pressure swing adsorption (pressure swing adsorption) or PSA in English)
• compressors as well as
• the steam reformer includes in these outlines:
• a radiation chamber it is equipped with tubes through which the mixture of hydrocarbons and water vapor are mixed, this is the place of the reforming reactions, the heat required for the reactions being supplied by heating the tubes via burners fed with fuel and air, - a convection chamber, it is the place of the convection chain, it recovers, via exchangers, the heat of the fumes generated in the radiation chamber; this heat serving in particular to generate the water vapor.
• the steam reforming step is frequently preceded by a pre-reforming step.
• the pre-reformer is directly linked to reformer and is not a separate functional element. This is the reason why it will not be considered in the rest of the description. It will be convenient to read the word reformer to understand reformer or group pre-reformer plus reformer.
• all the functional elements concerned constitutive units of production is distributed around a rack (rack in English language).
• This rack is in the form of a metal structure around which are arranged the various elements (functional elements and reformer); the space available under the rack is used for the passage of different incoming and outgoing fluids (electricity, gas, water, products, etc.) via pipes and pipelines, but also for the installation of various small equipment.
• the reformer whether of the "top fired” or “side fired” type, is a rectangular shaped element at its base, it is placed on a long side of the rack, parallel to it,
• the reformer is generally fueled at the rear, that is to say at the end of the reforming furnace, opposite the convection chain,
• the other functional elements (adsorption with pressure modulation or PSA, hydrodesulphurization or HDS, cooling of the synthesis gas, etc.) are situated on the other long side of the rack, perpendicular thereto,
• Useful fluids flow via piping along the rack. They are essentially powered and / or discharged at one end thereof, at the level of the battery limit, where the connection with the outside is made.
• the connecting lines (pipes, power supply) between the different functional units are arranged along the rack.
• the object of the present invention is a unit for producing a gas or a gaseous mixture obtained by treating a mixture of light hydrocarbons by reforming, of the type comprising at least one steam methane reformer.
• the unit according to the invention will have a lower construction cost thanks to an optimized use of the racks by a more complete operation of both the perimeter of the rack and its surface, optimized use that allows to reduce the size.
• the invention also makes it possible to reduce the lengths of collectors as well as piping and cables for the power supply, the civil engineering volumes located under the rack and the structure of the rack.
• the invention relates to a unit for the production and treatment of synthesis gas from a hydrocarbon mixture, comprising at least: a steam reformer,
• a rack of generally rectangular shape having two long sides of dimension L and two short sides, also called ends, for the distribution of said reformer and of said functional elements, as well as that of conduits for the transfer of gaseous, liquid and electric fluids, characterized in that the reformer is placed substantially perpendicular to the rack and at one end, and / or the functional elements are distributed on both sides of the L-size rack.
• the reformer being placed at one of the two ends of the rack, and along an axis substantially perpendicular thereto, the installation will be said arranged according to a "T" architecture.
• the fluids gaseous, liquid and electric
• the rack as described above is a rack of rectangular shape, having two long sides of dimension L, called long sides, and two small sides or ends. It is obvious that its shape may have minor variations and that in particular the rack may be supplemented by additional rack elements, since their surfaces are much lower than those of the main rack.
• at least functional elements being interconnected
• At least two interconnected functional elements are placed substantially face to face, on either side of the rack.
• One of the functional elements for the treatment of the hydrocarbon mixture upstream of the reformer may be a hydrodesulfurization module.
• one of the functional elements for the upstream treatment of the reformer is a pre-treatment module for naphtha (or naphtha module).
• the invention is particularly suitable for hydrogen production, so a preferred embodiment of the invention relates to a unit which comprises functional elements for the treatment of synthesis gas for the production of hydrogen.
• the plant for the production of hydrogen advantageously comprises all or part of the following functional elements:
• HDS hydrodesulfurization unit
• a module for cooling the synthesis gas a hydrogen purification module (PSA);
• PSA hydrogen purification module
• this relates to a unit characterized in that it comprises functional elements for the treatment of the synthesis gas in order to produce an H 2 / CO mixture.
• the installation may include in particular all or part of the following functional elements:
• this relates to a unit comprising functional elements for the treatment of synthesis gas in order to produce (also) carbon monoxide.
• a unit comprising functional elements for the treatment of synthesis gas in order to produce (also) carbon monoxide.
• it may include in addition to the above elements:
• the reformer is of the type comprising a radiation chamber and a convection chamber; it is typically a steam reformer.
• the reformer will advantageously be of the steam reformer type for the production of synthesis gas from a mixture of light hydrocarbons to be reformed comprising at least one reforming furnace containing reforming tubes for reforming the methane contained in said mixture as well as burners for supplying the heat necessary for reforming, feed means for said mixture to be reformed and for steam, means for feeding the furnace with fuel for supplying the fuel for the burners, a chain of convection for the recovery of fumes at the furnace outlet, wherein the fuel furnace supply means is located at the end of the furnace, convection chamber side, thereby limiting the length of the ducts.
• FIGS. 1A, 2A, 3A and 4A illustrate conventional architectures according to FIG. prior art
• Figures 1B, 2B, 3B and 4B illustrate architectures according to the invention.
• Figure 1A schematically shows an installation for producing and processing synthesis gas according to a known conventional arrangement.
• Figure 1 B schematically shows a comparable plant for production and treatment of synthesis gas arranged according to the "T" architecture of the invention.
• Figure 2A schematically shows the utility manifolds of the installation of Figure 1A.
• Figure 2B schematically shows the utilities collectors of the installation of Figure 1 B according to the invention.
• Figure 3A schematically shows the interconnections between the functional assemblies of the installation of Figure 1 A.
• FIG. 3B schematically shows the interconnections between the functional assemblies of the installation of FIG. 1B according to the invention.
• Figure 4A illustrates the particular case of a conventional installation for the production of hydrogen.
• Figure 4B illustrates the particular case of an installation equivalent to that of Figure 4A, but arranged according to the "T" architecture of the invention.
• the installation shown in Figure 1A includes:
• the reformer 1 A is arranged parallel to the rack 2 A , along one of the sides of length L A.
• the six functional assemblies 3 to 8 are arranged on the other side of the rack 2A , perpendicular to it.
• the installation according to the invention, shown in Figure 1 B, is comparable, it consists of the same number of elements of the same nature, that is to say: a reformer, a rack and the same six sous -sets or distinct functional assemblies, in which: - the reformer 1 B is a preferred reformer according to the invention: it is fed with fuel at the end of the convection oven chamber side, is substantially in its central part (it could be fed at its end, using suitable feeding means),
• the rack 1 B is of length L, substantially of length L A / 2, - the six subsets 3 to 8 are the same as those of Figure 1 A.
• the reformer 1 B according to the invention is placed perpendicularly to the rack at one of its ends, thereby freeing a rack in whole length L.
• the six functional units 3-8 can thus be distributed on both sides of the rack available 2 B of length L where they have a total length of rack 2 x L, equivalent to that they have in the arrangement according to Figure 1A.
• FIGS. 2A and 2B diagrammatically show the conduits intended to supply useful fluids to the reformer as well as the different functional assemblies 3 to 8 of the installations of FIGS. 1A and 1B.
• Useful fluids (cooling water, air instrumentation , nitrogen, steam, flare gas, etc.) thus flow via pipes grouped at the rack level.
• the pipes from the various elements among 1 B , and 3 to 8 join a collector called utility collector, disposed along the rack which therefore has a length substantially equal to that of the rack itself.
• These collectors distribute all useful fluids along the rack between the pipes dedicated to the functional units or the reformer and the means for supplying or discharging said useful fluids, means located at the end of the rack where is traditionally done with the customer. They also distribute the fluids that can be generated by one of the sets.
• FIGS. 3A and 3B schematically show certain interconnections between the different functional assemblies 3 to 8 constituting the installations of FIGS. 1A and 1B.
• the functional assembly 3 is interconnected with the functional assemblies 5 and 6
• the functional assembly 4 is interconnected with the functional assembly 8
• the functional assembly 5 is further interconnected with the functional assemblies 6 and 7.
• FIG. 3B where the reformer is placed at the end of the rack, and where the functional assemblies are distributed on either side of the rack, in accordance with the "T" architecture according to the invention, the cumulative length of pipes Rack is greatly reduced, especially when the elements are highly interconnected. In this case, a judicious distribution of functional elements on both sides of the rack, including some functional elements interconnected face to face allows to create direct links between these functional elements and thus to free up space at the rack .
• the installation for the production of hydrogen of Figure 4A is a typical installation comprising: a reformer 41A of the type supplied with fuel at the back in a known manner;
• a rack 42 A of length L 4A the following 5 functional units, referenced 43 to 47: • 43: a hydrodesulfurization unit (HDS) for the treatment of the hydrocarbon mixture upstream of the reformer,
• HDS hydrodesulfurization unit
• This plant is intended to produce hydrogen from a hydrocarbon source composed of natural gas and operates in the following manner: the natural gas GN feeds the hydrodesulfurization unit 43, and the outgoing desulfurized gas is introduced into a reformer 41 where it is reformed to provide a hot syngas.
• the hot synthesis gas passes into the cooling module 44 and is then introduced into the PSA purification module 45 to produce hydrogen.
• UH 2 product is mainly sent to the end of the rack towards the customer, a fraction of H 2 being sent to the set HDS 43 after compression in the compressor 46.
• the nitrogen starter module 47 feeds the reformer 41 A and the HDS 43 nitrogen for startup phases. A non-zero fraction of the natural gas supplied to the installation is used as fuel for the reformer in addition to the waste gas of the
• the reformer 41 A is arranged parallel to the rack 42 A , along one of the sides of length L 4A .
• the functional assemblies 43 to 47 are arranged on the other side of the rack, perpendicular to it.
• FIG. 4B The installation according to the invention, represented in FIG. 4B, is comparable, it consists of the same number of elements of the same nature, ie:
• a reformer 41 B but it is here of the preferred reformer type according to the invention, that is to say that it is fueled at the end of the convection chamber furnace, or substantially in its central part.
• HDS hydrodesulphurization unit
• Figure 4B works in the same way as in Figure 4A, ie as follows: this facility is intended to produce hydrogen from a natural gas source ; the natural gas GN feeds the hydrodesulphurization unit 43, then the desulphurized gas is introduced into the reformer 41 B where it is reformed to provide a hot synthesis gas. The hot synthesis gas passes into the cooling module 44 and is then introduced into the PSA purification module 45 to produce hydrogen. L 1 H 2 product is mainly sent to the end of the rack to the client a fraction of H 2 is sent to all HDS 43 after compression in the compressor 46. Furthermore, the module 47 feeds the reformer 41B as well as HDS 43 nitrogen for startup phases. A non-zero fraction of the natural gas supplied to the facility is used as fuel for the reformer in addition to the waste gas from the PSA.
• the reformer 41 B is a preferred reformer according to the invention: it is fueled at the end of the furnace on the convection chamber side, or substantially in its central part.
• the rack 42 B is of length L 4B, 4A is substantially L / 2,
• the five elements 43 to 47 are the same as those of FIG. 4A.
• the reformer 41 B according to the invention is placed perpendicularly to the rack, at one of its ends, thus completely releasing a length of rack L 4A / 2.
• the five functional elements can thus be distributed on both sides available the rack where they have thus twice the rack length L 48 , equivalent to L 4A (the one they have in the arrangement according to Figure 4A).
• the arrangement of the elements 43 to 47 is chosen judiciously so as to make the best use of the space available around the rack, but also so as to minimize the lengths of pipes.
• the element 46 (recycle compressor) which is placed substantially in front of the PSA 45 and substantially in front of I ⁇ DS 43.
• the length of the pipes conveying the different fluids is minimized partly by the placement of the elements relative to each other. to others, but also, and especially because the rack is twice as short as in the known classic solution.
• the arrangement of facilities for the steam reforming of a mixture of light hydrocarbons for the production of a synthesis gas and the treatment subsequent synthesis gas can significantly reduce the construction costs of the installation through the decrease:
• the invention can also be implemented for the production of carbon monoxide and / or a mixture of both, when using a reformer equipped with a oven and a convection chamber.

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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)
• Fuel Cell (AREA)

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• 2006
  • 2006-08-08 FR FR0653311A patent/FR2904820B1/fr active Active
• 2007
  • 2007-08-06 WO PCT/FR2007/051788 patent/WO2008017787A2/fr not_active Ceased
  • 2007-08-06 CN CN200780029463.9A patent/CN101500939B/zh not_active Expired - Fee Related
  • 2007-08-06 US US12/374,373 patent/US20090301309A1/en not_active Abandoned
  • 2007-08-06 JP JP2009523326A patent/JP2010500273A/ja active Pending
  • 2007-08-06 EP EP07823695A patent/EP2051932A2/de not_active Ceased

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