• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    Reactor-exchanger comprising at least 3 stages with on each floor at least one zone promoting heat exchange and at least one distribution zone upstream and / or downstream of the heat exchange promoting zone, characterized in that the zone Heat exchange favoring comprises cylindrical millimeter channels, said channels being in number from 1 to 1000 and length between 10 mm and 500 mm.
    公开号:FR3032783A1
    申请号:FR1551140
    申请日:2015-02-12
    公开日:2016-08-19
    发明作者:Pascal Del-Gallo；Olivier Dubet；Matthieu Flin；Laurent Prost；Marc Wagner
    申请人:Air Liquide SA；LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude；
    IPC主号:
    专利说明:

    [0001] The present invention relates to milli-structured reactor-exchangers, to their method of manufacture and to their use. A milli-structured reactor-exchanger is a chemical reactor where exchanges of matter and heat are intensified thanks to a geometry of channels whose characteristic dimensions such as the hydraulic diameter are of the order of a millimeter. These milli-structured reactor exchangers also make it possible to develop large exchange surfaces in a small volume, which makes them compact. The channels constituting the geometry of the milli-structured exchanger-reactors are of cylindrical shapes, this form is obtained by the production of this pressure apparatus by additive manufacturing under a powder bed or by powder spraying. "(i)" stage "means a set of channels positioned on the same level and in which a chemical reaction and / or heat exchange takes place, (ii)" wall "means a partition wall between two consecutive channels arranged on the same level, (iii) "distributor" or "distribution zone" means a volume connected to a set of channels and arranged on the same floor or a set of channels whose purpose is to channel the gas collectors and entering the reactor-exchanger or to convey to the collector the gases leaving the exchanger-reactor. (iv) "collector" means a volume connected to a set of channels and arranged on the same stage and in which circulates either the reagents conveyed from outside the exchanger-reactor to a set of channels or the products of the reaction fed from the set of channels to the outside of the exchanger-reactor (Figure 1). The operation of the reactor-exchanger is defined in Figure 1, the collectors bring and evacuate the gases; at the inlet, the hydrocarbon feedstock-steam mixture and at the outlet the synthesis gas produced. The coolant between 750 and 950 ° C brings the heat to the system for steam reforming a hydrocarbon feedstock. Three types of stage can be distinguished according to the fluid circulating in the channels of this stage: the stages comprising so-called "reactive" channels in which circulates, in the case of steam reforming, a mixture of hydrocarbon feedstock and water vapor, The stages comprising so-called "return" channels in which circulate the products of the steam reforming reaction. The products of the steam reforming reaction yield part of the heat necessary for the poreforming reaction to the hydrocarbon feed-steam mixture mixture. The stages comprising so-called "heat supply" channels in which a fluid circulates coolant to provide the heat necessary for the steam reforming reaction. A reactor exchanger consists of the stack of these three types of stages. The thermal integration of these devices can be subject to extensive optimization to optimize the heat exchange between the fluids circulating in the device at different temperatures through a spatial distribution of fluids on several floors and the use several distributors and collectors. To fully benefit from the benefits of using a milli-structured reactor exchanger or milli-structured exchanger in the industrial processes concerned, these equipment must have the following properties: - The possibility of being able to work on a product pressure x high temperature, the minimum values of which are generally of the order of 12 000 bar ° C. (corresponding to a minimum temperature of 600 ° C. and a minimum pressure of 1 bar to more than 20 bar). extremely high value of the surface / volume ratio, the typical values of which are between 40000 and 700 m2 / m3 and which allows the intensification of the phenomena at the walls and in particular the heat transfer for the heat exchange and the material transfer for 20 the reaction in the case of a reactor-exchanger. Moreover, these very high values of the surface-to-volume ratio make it possible to develop a considerable exchange surface with a small bulk of the equipment, compared to competing technologies (tubes and calenders, etc.). Several suppliers offer milli-structured reactor-exchangers, the majority of these devices consist of plates consisting of channels which are obtained by chemical machining by spraying or immersion. This method of manufacture leads to obtaining channels whose section has a shape that approaches a semicircle and whose dimensions are approximate and difficult to reproduce from one batch to another because of the method of machining itself. Indeed, during the chemical machining operation, the bath used 3032783 3/16 is polluted by the metal particles torn from the plates and although the latter is regenerated, it is difficult for reasons of operating cost to maintain the same efficiency when manufacturing a large series of plates. Subsequently, the term "semi-circular section" means the section of a channel whose properties suffer from the dimensional limits described above and induced by manufacturing methods such as chemical etching and stamping. Although this method of channel manufacturing is not economically attractive, it is conceivable that the channels constituting the plates are manufactured by traditional machining. In this case, the section of the latter would not semi-circular type 10 but rectangular, it will be called "rectangular section". The plates consisting of channels of semicircular or right angle sections thus obtained are generally assembled together by diffusion bonding or soldering diffusion. The sizing of these semi-circular or rectangular section devices is based on the application of the American Society of Mechanical Engineers (ASME) section VIII, paragraph 13, appendix 13.9 which incorporates the mechanical design of an exchanger and / or a milli-structured reactor-exchanger composed of etched plates. The values to be defined to obtain the desired mechanical strength are shown in Figure 2. The dimensioning of the distribution zone and the collector, of variable geometry (walls and channel widths), is performed by finite element calculation because the ASME code does not provides no analytical dimensioning of these areas.
    [0002] Once the design has been established, the regulatory validation of the design defined by this method requires a burst test according to ASME UG 101. For example, the expected burst value for a diffusion bonded and inconel alloy reactor heat exchanger (E1 R 120) operating at 25 bar and 900 ° C is of the order of 3500 bar at room temperature. This is very disadvantageous since this test requires the oversize of the reactor to comply with the burst test at room temperature, the reactor thus losing its compactness and its efficiency in terms of heat transfer due to the increase. walls of the channels. The manufacture of these exchangers and / or milli-structured exchanger is currently carried out according to the seven steps described in Figure 3. Among these steps, four are critical because they can cause problems of non-compliance having as only the disposal of the heat exchanger or the reactor exchanger or the plates constituting the pressure vessel if this non-conformity is detected early enough in the manufacturing line of these devices.
    [0003] These four steps are: - the chemical machining of the channels, - the assembly of the etched plates by soldering diffusion or diffusion welding, - the welding of the connection heads, on which welded tubes supply or discharge the fluids, on the distribution areas and the collectors and finally, 10 - the deposition operations of protective coatings and catalyst in the case of a reactor exchanger or exchanger subjected to a use inducing phenomena that can degrade the state of surface of the device. Whatever the machining method used for the manufacture of exchanger or milli-structured exchanger-reactor, one obtains semicircular section channels in the case of chemical machining (FIG. 4) and which consist of of two right angles or of rectangular section in the case of traditional machining and which consist of four right angles. This plurality of angles is detrimental to obtaining a homogeneous protective coating over the entire section. Indeed, geometric discontinuity phenomena such as angles increase the probability of generating inhomogeneous deposits, which will inevitably lead to the initiation of phenomena of degradation of the surface state of the matrix which one wants to preserve as for example phenomena of corrosion, carburetion or nitriding. The sections of angular channels obtained by chemical machining or traditional machining techniques do not optimize the mechanical strength of such an assembly.
    [0004] Indeed, the design calculations of the resistance to pressure of such sections result in an increase in the thickness of the walls and the bottom of the channel, the equipment thus losing its compactness but also its efficiency in terms of heat transfer. In addition, chemical machining imposes limitations in terms of geometric shapes such that no channel can be made having a height greater than or equal to its width, which leads to limitations in the ratio of surface area to volume resulting in optimization limitations. The assembly of the etched plates by diffusion welding is obtained by the application of a large uniaxial stress (typically of the order of 2 to 5 MPa) on the matrix consisting of a stack of etched plates and exerted by a high temperature press for a holding time of several hours. The implementation of this technique is compatible with the manufacture of small devices such as devices contained in a volume of 400 mm x 600 mm. Beyond these dimensions, the force to be applied to maintain a constant stress becomes too great to be implemented by a high temperature press. Some manufacturers using the diffusion welding process overcome the difficulties of implementing a significant constraint by using a so-called self-clamping assembly. This technique does not make it possible to effectively control the stress applied to the equipment, which generates crushing of channels. The assembly of the etched plates by diffusion brazing is obtained by the application of a low uni-axial stress (typically of the order of 0.2 MPa) exerted by a press or a self-clamping assembly at high temperature and for a time holding several hours to the matrix consisting of etched plates. Between each of the plates, a brazing filler metal is deposited according to industrial deposition processes which do not make it possible to guarantee the perfect mastery of this deposition. This filler metal is intended to diffuse into the matrix during the brazing operation so as to achieve mechanical joining between the plates. In addition, during the temperature maintenance of the equipment in manufacture, the diffusion of the brazing metal can not be controlled, which can lead to discontinuous brazed junctions and which result in a degradation of the mechanical strength of the solder. equipment. By way of example, the equipment manufactured according to the diffusion soldering method and dimensioned according to the ASME section VIII div.1 appendix 13.9 in HR120 that we realized did not resist the application of a pressure of 840 bar in the burst test 3032783 6/16. In order to overcome this degradation, the thickness of the walls and the geometry of the distribution zone have been adapted to increase the contact area between each plate. This has the effect of limiting the surface / volume ratio, increasing the pressure drop and the poor distribution in the channels of the equipment.
    [0005] In addition, the ASME code section VIII div.1 appendix 13.9 used for the sizing of this type of brazed equipment does not allow the use of soldering technology for equipment using fluids containing a lethal gas. such as carbon monoxide for example. Thus, a diffusion bonded apparatus can not be used for the production of Syngas.
    [0006] The equipment produced by diffusion brazing is ultimately composed of a stack of etched plates between which soldered joints are arranged. Therefore, any welding operation on the faces of this equipment leads in most cases to the destruction of soldered joints in the heat affected zone by the welding operation. This phenomenon propagates along the brazed joints and leads in most cases to the rupture of the assembly. To overcome this problem, it is sometimes proposed to add thick reinforcement plates at the time of assembly of the brazed matrix so as to provide a frame-type support welding connectors which does not have soldered joint. From a point of view of process intensification, the fact of assembling engraved plates between them forces to realize a design of the equipment according to a two-dimensional approach which limits the thermal and fluidic optimization within the exchanger or the exchanger-reactor by requiring the designers of this type of equipment to be limited to a floor approach of the distribution of fluids. From an eco-manufacturing point of view, all these manufacturing steps are performed by different business skills are generally performed at various subcontractors located in different geographical locations. This results in long lead times and many parts transport. From this, a problem is to provide an improved reactor-exchanger not having at least some of the disadvantages mentioned above. A solution of the present invention is a reactor-exchanger comprising at least 3 stages with on each stage at least one zone promoting heat exchange and at least one distribution zone upstream and / or downstream of the zone. promoting heat exchange, characterized in that the heat exchange promoting zone comprises cylindrical 5 millimeter channels, said channels being 1 to 1000 in number and 10 mm to 500 mm in length. Depending on the case, the reactor-exchanger according to the invention may have one or more of the following characteristics: the distribution zone comprises millimetric channels which correspond to the continuous extension of the channels of the zone favoring the exchange of heat; of the same floor are separated by walls with a thickness of less than 2 mm. the channels have a hydraulic diameter of between 0.5 and 3 mm, the channels have a length of between 50 and 400 mm, preferably between 100 and 300 mm, and the reactor exchanger comprises a reaction stage. whose channels are able to promote a reaction by allowing in particular the circulation of reactive gas flows, a "return" stage whose channels allow the circulation of gas flows produced, a "heat input" stage whose channels allow the circulation of a coolant. the number of channels in the "reaction" stage is between 100 and 700, preferably between 200 and 500, the number of channels in the "return" stage is between 100 and 700, preferably between 200 and 500, the number of channels in the "heat input" stage is between 100 and 700, preferably between 200 and 500, the "reaction" stage is surrounded by a level " of "heat input" and a "return" level - the channels of the "reaction" stage and the channels of the "return" stage have on at least a portion of their internal walls a protective coating against corrosion. - The channels of the "reaction" stage have on at least a portion of their internal walls a catalyst. It should be noted that the protective coating and the catalyst are preferably deposited by a liquid route.
    [0007] The present invention also relates to the manufacture of the reactor-exchanger according to the invention. An additive manufacturing method is preferably used to manufacture a reactor-exchanger according to the invention. Preferably, the additive manufacturing method uses as basic material at least one metal powder of micrometric size. The additive manufacturing method can employ micron-sized metal powders that are melted by one or more lasers to produce finished parts of complex three-dimensional shapes. The part is built layer by layer, the layers are of the order of 50 ptm, depending on the accuracy of the desired shapes and the desired deposition rate. The metal to be melted can be supplied either by powder bed or by a spray nozzle. The lasers used for locally melting the powder are either YAG, fiber or CO2 lasers and the melting of the powders takes place under an inert gas (argon, helium, etc.). The present invention is not limited to a single additive manufacturing technique but it applies to all known techniques. In contrast to chemical machining or traditional machining techniques, the additive manufacturing method makes it possible to produce cylindrical section canals which have the following advantages (FIG. 4): (i) to offer better resistance to pressure and thus to allow a significant reduction in the thickness of the walls of the channels and (ii) to allow the use of dimensioning rules of pressure vessels that do not require the completion of a burst test to prove the effectiveness of the design as is the case for Section VIII Div.1 Appendix 13.9 of the ASME Code.
    [0008] Indeed, the design of an exchanger or exchanger-reactor made by additive manufacturing, making it possible to produce channels with a cylindrical section (FIG. 5), is based on "usual" design rules for apparatus to pressure that apply to the sizing of the channels, distributors and collectors with cylindrical sections constituting the exchanger-reactor or the milli-structured exchanger. By way of example, the dimensioning of the wall of straight rectangular section channels (value t3 in FIG. 2) of a nickel alloy reactor-heat exchanger (HR 120), dimensioned according to ASME (American Society of Mechanical Engineers) Section VIII Div.1 Appendix 13.9, is 1.2 mm. By using cylindrical section channels, this wall value calculated by the ASME section VIII div.1 5 is only 0.3 mm, a reduction by four of the wall thickness required for the resistance to pressure. . The reduction in the volume of material related to this gain makes it possible (i) to reduce the size of the apparatus with identical production capacity by the fact that the number of channels necessary to reach the production capacity concerned is smaller and thus occupies less space, (ii) 10 or increase the production capacity of the device while maintaining the size of the latter which allows to position more channels and thus treat a larger flow of reagents. In addition, in the case of exchanger-reactor or milli-structured exchanger made of noble alloy with a high nickel content, the reduction of material necessary goes in the direction of eco-design which is beneficial for the environment while reducing the cost of raw materials. The techniques of additive manufacturing ultimately allow to obtain so-called "massive" parts which in contrast to assembly techniques such as diffusion brazing or diffusion welding do not have interfaces of assemblies between each etched plate. This property goes in the direction of the mechanical strength of the device by eliminating by construction the presence of weakening lines and thereby eliminating a source of potential fault. Obtaining massive parts by additive manufacturing and the elimination of soldering or diffusion welding interfaces makes it possible to envisage numerous design possibilities without being limited to wall geometries designed to limit the impact of possible defects in the design. assembly such as discontinuities in the brazed joints or in the welded-diffused interfaces. The additive manufacturing makes it possible to achieve unimaginable forms by the traditional manufacturing methods and thus the manufacture of the connectors of the exchangers-reactors or milli-structured exchangers can be done in the continuity of the manufacture of the body of the 3032783 10/16 devices. This then makes it possible not to perform welding of the connectors on the body and thus eliminate a source of alteration of the structural integrity of the equipment. The mastery of the geometry of the channels by additive manufacturing allows the realization of circular section channels which, besides the good pressure resistance that this shape brings, also allows to have an optimal channel shape for the deposition of protective coatings and catalysts which are thus homogeneous throughout the channels. By using this additive manufacturing technology, the productivity gain aspect is also enabled by reducing the number of manufacturing steps. In fact, the steps of producing a reactor by integrating the additive manufacturing go from seven to four (FIG. 6).
    [0009] The critical steps, which can generate a scrapping of a complete apparatus or plates constituting the reactor, four in number using the conventional manufacturing technique by assembly of etched plates, are passed to two with the adoption of the additive manufacturing. Thus, the only remaining steps being the additive manufacturing step and the deposition step of coatings and catalysts.
    [0010] In summary, the advantages of additive manufacturing over a conventional soldering or diffusion bonding solution for chemically etched plates are: - greater process intensification (channel integration, compactness) - reduction of reactor weight or increase the volume that is useful for the catalytic reaction - a reduction in the number of manufacturing steps and intervening agents located at different sites - an improvement in the quality of manufacture by ensuring perfect reproducibility - a possible control of the process during manufacture, This will reduce the amount of parts being discarded - a simplification of design validation according to the ASME Construction Code. The exchanger-reactor according to the invention is particularly suitable for use in a steam reforming process, preferably for the production of hydrogen having a flow rate of between 0.1 and 10 Nm3 / h, preferably between 1 and 5 Nm3 / h. Within this framework of a hydrogen production lower than 5 Nm3 / h, we can take the example of a reactor-Inconel 625 exchanger for the production of 0.6 Nm3 / h of hydrogen intended to feed a fuel cell to produce electricity and hot water 3032783 of a dwelling. The dimensional characteristics for this reactor-exchanger would be as follows: - Materials of nickel base type (Inconel 601 - 625 617 - 690) - Channels of 1.14 mm diameter 5 - Wall of 0.4 mm - Effective length of channels 150 mm - Number of "reactive" channels 232 - Number of "return" channels 116 - Number of "heat transfer" channels 174 10 - Width of the reactor exchanger 49 mm - Total length of the reactor exchanger 202 mm - Height 25.4 mm reactor-exchanger - "reactive" channels and "return" channels are coated with corrosion protection - "reactive" channels are coated with catalyst 15 From the following inlet conditions: Reactive gas Smoke Flow N m3 / h 0.70 2.01 Temperature ° C 368.5 900 Pressure bar 1.1 1.1 Composition CH4 0.2050 0.0000 C2 0.0000 0.0000 H20 0.6149 0.1149 02 0.0000 CO2 0.0439 0.0307 H2 0.1357 0.0000 CO 0.0005 0.0000 N2 0.0000 0.7213 3032783 12/16 The equipment previously described allows to' achieve the following performance: Gas produced Smoke Flow Nm3 / h 0.97 2.01 Temperature ° C 439 460 Pressure bar 1.1 1.1 Composition (mol CH4 0.01 0.0000 basis) C2 0.0000 0.0000 H20 0.31 0.1149 02 0.0000 0.1331 CO2 0.030 0.0307 H2 0.51 0.0000 CO 0.14 0.0000 N2 0.0000 0.7213 Pressure loss mbar 6.19 10.76
    权利要求:
    Claims (16)
    [0001]
    REVENDICATIONS1. Reactor-exchanger comprising at least 3 stages with on each floor at least one zone promoting heat exchange and at least one distribution zone upstream and / or downstream of the heat exchange promoting zone, characterized in that the zone Heat exchange favoring comprises cylindrical millimeter channels, said channels being in number from 1 to 1000 and length between 10 mm and 500 mm.
    [0002]
    2. Reactor-exchanger according to claim 1, characterized in that the distribution zone comprises millimeter channels which correspond to the continuous extension of the channels of the zone promoting heat exchange
    [0003]
    3. Reactor-exchanger according to one of claims 1 or 2, characterized in that the channels of the same stage are separated by walls with a thickness of less than 2 mm.
    [0004]
    4. Reactor-exchanger according to one of claims 1 to 3, characterized in that the channels have a hydraulic diameter of between 0.5 and 3 mm.
    [0005]
    5. Reactor-exchanger according to one of claims 1 to 4, characterized in that the channels are of length between 50 and 400 mm, preferably between 100 and 300 mm,
    [0006]
    6. Reactor-exchanger according to one of claims 1 to 5, characterized in that said exchanger-reactor comprises: - a stage of "reaction" whose channels are able to promote a reaction including allowing the circulation of gaseous reactive flows - a "return" stage whose channels allow the circulation of gas flows produced, - a "heat input" stage whose channels allow the circulation of a heat transfer fluid. 3032783 14/16
    [0007]
    7. Reactor-exchanger according to claim 6, characterized in that the number of channels in the "reaction" stage is between 100 and 700, preferably between 200 and 500. 5
    [0008]
    8. Reactor-exchanger according to one of claims 6 or 7, characterized in that the number of channels in the "return" stage is between 100 and 700, preferably between 200 and 500.
    [0009]
    9. Reactor-exchanger according to one of claims 6 to 8, characterized in that the number of channels in the "heat input" stage is between 100 and 700, preferably between 200 and 500.
    [0010]
    10. Reactor-exchanger according to one of claims 6 to 9, characterized in that the "reaction" stage is surrounded by a level of "heat input" and a level of "return". 15
    [0011]
    11. Reactor-exchanger according to one of claims 6 to 10, characterized in that the channels of the "reaction" stage and the channels of the "return" stage have on at least a portion of their internal walls. a protective coating against corrosion.
    [0012]
    12. Reactor-exchanger according to one of claims 6 to 11, characterized in that the channels 20 of the "reaction" stage have on at least a portion of their inner walls a catalyst.
    [0013]
    13. Use of an additive manufacturing method for the manufacture of a reactor-exchanger according to one of claims 1 to 12. 25
    [0014]
    14. Use according to claim 13, characterized in that the additive manufacturing method uses as basic material at least one metal powder of micrometric size. 3032783 15/16
    [0015]
    15. Process for steam reforming a hydrocarbon feedstock using a reactor-exchanger according to one of claims 1 to 12.
    [0016]
    16. A method of steam reforming according to claim 15 comprising a production of hydrogen having a flow rate of between 0.1 and 10 Nm3 / h, preferably between 1 and 5 Nm3 / h.
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    同族专利:
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    引用文献:
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    FR3060553B1|2016-12-15|2021-02-19|Air Liquide|EXCHANGER-REACTOR INCLUDING CONNECTORS WITH SUPPORTS|
    FR3064348B1|2017-03-24|2019-04-05|L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude|HEAT EXCHANGER COMPRISING CONNECTORS WITH SUPPORTS|
    AT521830B1|2018-11-05|2021-07-15|Avl List Gmbh|Method of making a gas processing device|
    FR3096768B1|2019-05-29|2021-04-30|Air Liquide|Exchanger-reactor with improved distribution zones|
    WO2021042023A1|2019-08-31|2021-03-04|Corning Incorporated|Improved heat exchange flow reactor|
    WO2021168583A1|2020-02-28|2021-09-02|Societe de Commercialisation des Produits de la Recherche Appliquée Socpra Sciences et Génie S.E.C.|Integrated micro-reactors for hydrogen synthesis via methane reforming|
    法律状态:
    2016-02-18| PLFP| Fee payment|Year of fee payment: 2 |
    2016-08-19| PLSC| Publication of the preliminary search report|Effective date: 20160819 |
    2017-02-17| PLFP| Fee payment|Year of fee payment: 3 |
    2018-02-23| PLFP| Fee payment|Year of fee payment: 4 |
    2020-02-19| PLFP| Fee payment|Year of fee payment: 6 |
    2021-02-24| PLFP| Fee payment|Year of fee payment: 7 |
    2022-02-16| PLFP| Fee payment|Year of fee payment: 8 |
    优先权:
    申请号 | 申请日 | 专利标题
    FR1551140A|FR3032783B1|2015-02-12|2015-02-12|MILL-STRUCTURE REACTOR EXCHANGER FOR HYDROGEN PRODUCTION LESS THAN 10 NM3 / H|FR1551140A| FR3032783B1|2015-02-12|2015-02-12|MILL-STRUCTURE REACTOR EXCHANGER FOR HYDROGEN PRODUCTION LESS THAN 10 NM3 / H|
    CA2976280A| CA2976280A1|2015-02-12|2016-02-03|Millimeter-scale exchanger-reactor for hydrogen production of less than 10 nm3/h|
    CN201680008774.6A| CN107223070A|2015-02-12|2016-02-03|Grade exchanger reactor for the hydrogen gas production less than 10Nm3/h|
    KR1020177023048A| KR20170116052A|2015-02-12|2016-02-03|Millimeter-size exchangers for the production of hydrogen below 10 < RTI ID = 0.0 > NM3 /|
    PCT/FR2016/050229| WO2016128647A1|2015-02-12|2016-02-03|Millimetre-scale exchanger-reactor for hydrogen production of less than 10 nm3/h|
    US15/550,618| US20180170750A1|2015-02-12|2016-02-03|MILLIMETER-SCALE EXCHANGER-REACTOR FOR HYDROGEN PRODUCTION OF LESS THAN 10 Nm3/h|
    BR112017016687A| BR112017016687A2|2015-02-12|2016-02-03|millimeter-scale heat exchanger-reactor for a hydrogen production of less than 10 nm3 / h|
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