WO2008132313A2 - Réacteur échangeur compact utilisant une pluralité de brûleurs poreux - Google Patents
Réacteur échangeur compact utilisant une pluralité de brûleurs poreux Download PDFInfo
- Publication number
- WO2008132313A2 WO2008132313A2 PCT/FR2008/000293 FR2008000293W WO2008132313A2 WO 2008132313 A2 WO2008132313 A2 WO 2008132313A2 FR 2008000293 W FR2008000293 W FR 2008000293W WO 2008132313 A2 WO2008132313 A2 WO 2008132313A2
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- WIPO (PCT)
- Prior art keywords
- tubes
- exchanger
- reactor
- reactor according
- exchanger reactor
- Prior art date
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Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23D—BURNERS
- F23D14/00—Burners for combustion of a gas, e.g. of a gas stored under pressure as a liquid
- F23D14/12—Radiant burners
- F23D14/16—Radiant burners using permeable blocks
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/06—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds in tube reactors; the solid particles being arranged in tubes
- B01J8/067—Heating or cooling the reactor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/06—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds in tube reactors; the solid particles being arranged in tubes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/06—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds in tube reactors; the solid particles being arranged in tubes
- B01J8/062—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds in tube reactors; the solid particles being arranged in tubes being installed in a furnace
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C99/00—Subject-matter not provided for in other groups of this subclass
- F23C99/006—Flameless combustion stabilised within a bed of porous heat-resistant material
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23D—BURNERS
- F23D14/00—Burners for combustion of a gas, e.g. of a gas stored under pressure as a liquid
- F23D14/20—Non-premix gas burners, i.e. in which gaseous fuel is mixed with combustion air on arrival at the combustion zone
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00504—Controlling the temperature by means of a burner
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C2900/00—Special features of, or arrangements for combustion apparatus using fluid fuels or solid fuels suspended in air; Combustion processes therefor
- F23C2900/03002—Combustion apparatus adapted for incorporating a fuel reforming device
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C2900/00—Special features of, or arrangements for combustion apparatus using fluid fuels or solid fuels suspended in air; Combustion processes therefor
- F23C2900/9901—Combustion process using hydrogen, hydrogen peroxide water or brown gas as fuel
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23D—BURNERS
- F23D2203/00—Gaseous fuel burners
- F23D2203/10—Flame diffusing means
- F23D2203/101—Flame diffusing means characterised by surface shape
- F23D2203/1012—Flame diffusing means characterised by surface shape tubular
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23D—BURNERS
- F23D2203/00—Gaseous fuel burners
- F23D2203/10—Flame diffusing means
- F23D2203/105—Porous plates
- F23D2203/1055—Porous plates with a specific void range
Definitions
- the invention relates to a novel exchanger reactor for carrying out highly endothermic chemical reactions, such as steam reforming reactions of naphtha or natural gas.
- the exchanger reactor is understood to mean a chemical reactor in which the reaction (s) takes place inside a bundle of tubes enclosed in a shell, the energy required for the reactions being provided by a hot fluid circulating inside said shell. shell and outside the tubes, and giving up its heat to the reaction tubes essentially by convection.
- the energy is provided by the combustion of a fuel optionally containing hydrogen, said combustion occurring inside the exchanger reactor itself and generating combustion fumes which, for a part, give up their energy mainly by radiation, and, for another part, mainly by convection.
- a fuel optionally containing hydrogen
- combustion fumes which, for a part, give up their energy mainly by radiation, and, for another part, mainly by convection.
- the term "mainly” means a radiation contribution of at least 70% in the so-called radiation zone, and a convective contribution of at least 70% in the so-called convection zone.
- the novelty of the exchanger reactor according to the invention therefore lies in the existence of a heating zone of the reaction tubes in which the heat transfer is obtained mainly by radiation.
- the burners equipping the exchanger reactor according to the invention are burners without pre-mixing, of cylindrical geometry, and having a porous element separating the fuel side from the combustion side, the combustion taking place either inside said porous element, or in the vicinity its outer surface and to generate in the latter case a flat flame.
- porous burners to designate the specific burners used in the exchanger reactor according to the invention. A complete description of these porous burners can be found in the patent application 06 / 10,999.
- the fuel used in the context of the present invention may be a gaseous fuel based on hydrocarbons, such as natural gas. It may in some cases contain hydrogen, or even in some cases be essentially hydrogen.
- the oxidant may be any gas containing oxygen, in particular air, but also enriched or depleted oxygen air.
- the oxidant can even in a particular case be pure oxygen.
- the exchanger reactors can be defined as a category of reactors in which the energy required for chemical reactions is provided by a hot fluid, the heat exchange between said hot fluid and the charge to be treated circulating inside a plurality of tubes, being essentially by convection. Most often, the exchanger reactors are of low capacity (of the order of 1000 to 5000 Nm3 / h of H2 production), and used for small local productions.
- An example of a small capacity exchanger reactor is the reactor described in the patent application WO2001056690, or in US Pat. No. 4,919,844.
- the reactor according to the present invention is a heat exchanger reactor that can produce small quantities of products.
- hydrogen as those of the prior art, but also achieve large capacities, of the order of 100,000 Nm3 / h of H2 production, such as those commonly achieved in steam reforming furnaces.
- the exchanger reactor according to the invention is therefore an exchanger reactor with in situ combustion heat generation, using a specific burner to generate a flat flame, and to cover hydrogen production capacities ranging from 500 to 100,000. Nm3 / h.
- the patent application WO 2007 000 244 A1 describes a small capacity exchanger reactor intended for hydrogen productions of the order of 1000 Nm 3 / hour and comprising a first zone for generating heat by means of a burner, followed by a second convective exchange zone between the combustion fumes generated in the first zone and tubes within which the reaction mixture circulates.
- the zone of heat generation by means of a burner does not contain reaction tubes, and the burner is a conventional burner.
- US Patent 6,136,279 discloses a steam reforming furnace comprising a cylindrical envelope enclosing a plurality of tubes to be heated and a burner itself contained in a casing internal to the cylindrical envelope and defining a combustion chamber. The inner envelope containing the burner is separated from the tubes to be heated in such a way that the tubes do not see the flame and are heated only by the convection of the hot fumes.
- FIG. 1 represents a profile section of the exchanger reactor according to the invention.
- FIG. 2 represents a horizontal section of the exchanger reactor which makes it possible to visualize the relative arrangement of the tubes and the burners,
- FIG. 3 represents a porous burner used in the exchanger reactor according to the invention.
- the exchanger reactor according to the present invention is intended for the implementation of highly endothermic reactions and at temperatures up to
- 950 0 C Typically, it can be used for the steam reforming of hydrocarbon fractions, including naphtha or natural gas for hydrogen production.
- the burners used have in fact a fuel distributor which is designed in the form of several sections each having a given orifice diameter so as to allow modulation of the heat flow along the longitudinal axis of the burner which coincides with the longitudinal axis tubes to be heated, and with the longitudinal axis of the exchanger reactor itself.
- the resulting flame is a "flat" flame that allows combustion much more homogeneous than a traditional flame (that is, developing in a volume of 3 dimensions more or less well controlled).
- This flat flame considerably reduces the risk of hot spots, which is a particularly important aspect with regard to the operational safety of this type of reactor using pressure tube up to several tens of bars, and generating effluents containing hydrogen.
- the exchanger reactor according to the invention can therefore be defined as an exchanger reactor for the implementation of highly endothermic reactions. It consists of a shell of generally cylindrical shape (1) closed in its upper part by a cap (2) of substantially ellipsoidal shape and in its lower part by a bottom (3) of substantially ellipsoidal shape, said calender (1 ) enclosing a plurality of vertical tubes (4) of length Lt which extend along the cylindrical portion of the shell (1).
- the reactive fluids circulate inside the tubes (4), said tubes having at least one end communicating with the outside of the exchanger reactor, and said tubes being heated by a plurality of porous burners without premixing (7) of length Lb, extending vertically between the tubes to be heated (4) so that the ratio Lb / Lt is between 0.1 and 0.8 and preferably between 0.2 and 0.7.
- the center-to-center distance between a given burner and the neighboring tube or tubes is generally between 100 mm and 500 mm.
- the ratio H / D between the height H of the reactor and its diameter D is generally between 1 and 10, and preferably between 2 and 8.
- the tubes to be heated (4) are preferably bayonet tubes, the entry of the reagents and the effluent outlet can be done in the upper part of the reactor (I), the fuel distribution in the porous burners (7) then being located in the lower part (II) of the reactor.
- the convection heating zone is generally equipped with a baffle making it possible to obtain a flue gas circulation rate along the tube to be heated, generally between 5 m / s and 60 m / s, and preferably between 20 m / s and 50 m / s.
- the number of tubes to be heated per m 2 of section of the reactor is generally between 4 and 17, and preferably between 5 and 13.
- reactor section is meant the geometric section supposed to be empty of any internal.
- the tubes most often form a triangular pitch with a center-to-center distance preferably between 2 and 4 times the inside diameter of the tube.
- the tubes are of the bayonet type, they most often form a triangular pitch with a center-to-center distance preferably between 2 and 4 times the inside diameter of the outer envelope (6).
- the flue gas circulation zone may in some cases, in its upper part, comprise a deflection plate (14) located at a distance of at least 5 cm from the tubular plate (15) that it protects.
- the fuel used in the porous burners is generally a gaseous fuel of any chemical composition, such as in particular natural gas. It may in certain cases contain a part of the reaction effluent, after reaction of conversion of CO into CO2 and elimination of said CO2 and water. In some cases, it may consist of hydrogen in a molar proportion ranging from 5% to 100%, that is to say that it may optionally consist of pure hydrogen.
- the invention also relates to a steam reforming process using the exchanger reactor according to the invention, and preferably using as a natural gas feed for the production of hydrogen.
- the exchanger reactor is composed of an outer casing comprising an approximately vertical cylindrical part (1), completed in its upper part by a cap of approximately ellipsoidal shape (2), and in its lower part by a bottom
- the shell encloses a plurality of tubes (4) extending along the vertical axis of the reactor, and having a reagent distribution member (8) and an effluent collection member (11) passing through the shell and allowing the communication said reactor with the outside.
- Figure (1) shows bayonet type tubes having the inlet (8) of the reactive fluids and the outlet (11) effluents located on the same upper end of the reactor.
- this representation is not limiting, and the entry and exit of the reactive fluids could be located at the lower end of the reactor.
- bayonet tube is the type of tube preferred in the context of the present invention, but the reactor according to the invention can also operate with simple tubes having their inlet and outlet located at the upper end (/ or respectively lower /), the other at the lower end (/ or respectively upper /) of said reactor.
- the bayonet tubes (4) of the fluid to be treated consist of a cylindrical outer casing (6) inside which there is a tube (5) open at its upper end opening into the upper part (I) of the reactor, and open at its lower end opening into the cylindrical envelope (6).
- the inlet of the fluid to be treated is through the upper part (III) of the reactor by means of a dispensing member having at least one opening (8) communicating with the fluid. outside the exchanger reactor, allowing the entry of the fluid to be treated, and having a plurality of openings communicating directly with the annular portion of the tubes (4).
- the zone (III) is between the first tube plate (15) to which the outer shells (6) of the tubes (4) and the second tube plate (16) to which the inner tubes (5) are attached are fixed.
- the annular zone of the tubes (4) is delimited by the inner wall of the envelope (6) and the outer wall of the inner tube (5), said annular zone being generally filled with catalyst.
- the steam reforming catalyst is generally based on nickel and is most often in the form of small cylinders with a diameter of between 8 mm and 15 mm and a height of between 5 mm and 10 mm.
- the invention is in no way related to a type of catalyst or to a particular form of the latter.
- the fluid to be treated flows down the annular zone to its lower end, then passes after a 180 ° turn in the interior of the inner tube (5).
- the fluid to be treated goes up along said inner tube (5), the upper end of which opens into the upper part (I) of the exchanger reactor.
- the fluid to be treated is first heated on a length Lc mainly by convection, then secondly heated over a length Lr mainly by radiation.
- the zones corresponding to the length Lc and to the length Lr are respectively called convective zone and radiative zone.
- the portion Lc corresponding to the convection heating may comprise a baffle or any other equivalent system (12) for accelerating the combustion fumes in a direction substantially parallel to the length of the tubes (4) so as to promote the exchange of heat by convection.
- the longitudinal velocity of the fumes along the convective zone is between 5 m / s and 60 m / s, and more preferably between 10 m / s and 50 m / s.
- Figure 3 is a schematic view of a porous burner used in the exchanger reactor according to the present invention.
- the porous burners used in the exchanger reactor according to the invention are pre-mixed burner, of cylindrical geometry, length Lb and diameter Db, with a ratio Lb / Db generally between 10 and 500, and preferably between 30 and 300.
- These burners have a central fuel distributor (17) having a non-uniform orifice distribution (20), and have a porous annular member (18) surrounding the central distributor (17) at least over its entire length Lb , the thickness of said porous element (18) being preferably between 0.5 and 5 cm, and the inner surface of said porous material (18) being preferably located at a distance from the central distributor (17) of between 0.5 cm and 10 cm. This is precisely the distance corresponding to the noted area (19) in FIG.
- the porosity of the porous element (18) is generally less than 50%, and preferably less than 30%. This porosity is defined as the empty volume relative to the apparent volume of the porous element. Most often this porosity is homogeneous over the entire porous element, but in some cases, it can be differentiated, that is to say, have a different value according to several zones of said porous element.
- the porous burners (7) used in the present invention have a central distributor (17) which can have a single section with a single orifice diameter or be divided into at least two sections, each section having orifices (20) likewise diameter, and the different sections having diameters different from one to the other.
- the central distributor (17) can be divided into at least two sections, each section having orifices (20) of increasing diameter with the axial distance along the distributor in the direction of flow of the fuel.
- the central distributor (17) can be divided into at least two sections, each section having orifices (20) of increasing diameter according to a law of exponential type in the direction of fuel flow.
- This arrangement makes it possible to achieve, throughout the porous burner (7), an approximately constant heat flow, which would not be the case with a single orifice diameter, because of the pressure drop along the distributor which would necessarily lead to a lower fuel flow rate on the orifices furthest from the fuel introduction end in said distributor.
- This aspect is all the more important in the context of the present invention that porous burners can have lengths Lb of 10 m or more, and up to 15 meters.
- the porous burners (7) are supplied with fuel (noted (H) in FIG. 3) by the dispensing member (9), which may be of any type known to those skilled in the art, for example in the form of a rake, so as to uniformly feed the plurality of porous burners (7).
- the present invention is in no way related to any particular type of fuel dispenser.
- the burners (7) extend vertically over a length Lb and are arranged in such a way that the distance between a given burner and the tube (s) to be heated is preferably between 100 mm and 700 mm and more preferably between 150 mm and 500 mm. This distance is defined as the distance separating the burner axis from the axis of the tube, called the "center-to-center" distance.
- the length Lb of the porous burners is related to the length Lt of the tubes to be heated, and will generally be between 0.1 and 0.8 times the length of said tubes, and preferably between 0.2 and 0.7 times the length tubes. Given the length of the tubes to be heated, the length of the porous burners will generally be between 2 and 15 meters, and preferably between 4 and 12 meters.
- FIG. 2 shows a typical arrangement of tubes to be heated (4) and porous burners (7) in the particular case where the tubes are organized in a triangular pitch with a center-to-center distance between tubes equal to 3 times the inner diameter of the outer casing (6) of the tubes (4).
- FIG. 2 is in no way limiting of the various distribution configurations that the burners (7) and the tubes (4) can take.
- the tubes can in some cases form a square step.
- the preferred configuration is that of tubes forming a triangular pitch.
- the fuel may be of any type available on the site where the exchanger reactor is installed, most often a refinery or a petrochemical complex.
- the fuel may be natural gas or a gas from the purge of certain units of the refinery (called "off gas" in the English terminology that can be translated purge gas).
- the fuel may contain hydrogen in a proportion of between 5% and
- the fuel may also consist of a part of the production of the H2-rich gas, exchanger reactor effluent after reaction of conversion of CO to CO2, extraction of said CO2 and condensation of water.
- the fuel may consist in part of a fraction of the reaction effluent of the exchanger reactor.
- the oxidant generally air optionally enriched with oxygen, is admitted through the pipe (10) located in the lower part of the reactor.
- the combustion takes place generally on the surface of the porous element constituting the burner
- the side facing the region (III) being at the inlet temperature reactive fluids is a temperature generally between 300 0 C and 550 0 C
- the side facing the region (I) being at a temperature close to the outlet temperature of the reaction effluents a temperature generally between 550 0 C and 850 ° C.
- a protective plate (14) substantially parallel to the tubular plate (15) is therefore installed upstream of said tubular plate (15) so as to provide thermal protection for said plate (15).
- the flue gases are discharged from the exchanger reactor via the outlet pipe (13), preferably located between the protection plate (14) and the baffle (12).
- Example 1 Sizing of an exchanger reactor according to the invention with a hydrogen production capacity of 7000 Nm3 / hour.
- the exchanger reactor is designed to produce 7000 Nm3 / hour of hydrogen by steam reforming of natural gas.
- the fuel used is a refinery purge gas which has the following molar composition:
- the fuel flow is 150 km / h: Total reactor height (with upper and lower bottoms): 15m Reactor diameter: 2m H / D ratio: 7.5 Tubes are bayonet type Tube length: 12m External diameter of the tubes to be heated: 200mm Outside diameter of the inner tube: 40mm Outside diameter of the porous burners: 100mm Length of the porous burners: 5m Distance between centers of the tubes to be heated: 300mm Number of tubes: 19 tubes distributed in triangular pitch Number of porous burners: 36
- the exchanger reactor is designed to produce 90,000 Nm3 / hour of hydrogen by steam reforming of natural gas.
- the fuel used is a part of the effluent of the exchanger reactor after conversion reaction of CO into CO2 and water uptake.
- the fuel has the following composition in mol%: H 2: 92.10% CH 4: 5.35% CO 2: 0.78% CO: 1.5% N 2: 0.25%.
- the tubes are bayonet type
- Tube length 12m External diameter of the tubes to be heated: 200mm
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Hydrogen, Water And Hydrids (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
Description
Claims
Priority Applications (5)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP20080775633 EP2132486B1 (fr) | 2007-03-30 | 2008-03-05 | Réacteur échangeur compact utilisant une pluralité de brûleurs poreux et procedes utilisant ce reacteur |
CA2679528A CA2679528C (fr) | 2007-03-30 | 2008-03-05 | Reacteur echangeur compact utilisant une pluralite de bruleurs poreux |
KR1020097019587A KR101426979B1 (ko) | 2007-03-30 | 2008-03-05 | 복수 개의 다공 버너를 이용하는 컴팩트한 교환기-반응기 |
US12/593,510 US8834586B2 (en) | 2007-03-30 | 2008-03-05 | Compact exchanger-reactor using a plurality of porous burners |
JP2010501548A JP5298118B2 (ja) | 2007-03-30 | 2008-03-05 | 複数の多孔性バーナを用いたコンパクトな交換器−反応器 |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR0702410A FR2914395B1 (fr) | 2007-03-30 | 2007-03-30 | Nouveau reacteur echangeur compact utilisant un bruleur poreux |
FR0702410 | 2007-03-30 |
Publications (2)
Publication Number | Publication Date |
---|---|
WO2008132313A2 true WO2008132313A2 (fr) | 2008-11-06 |
WO2008132313A3 WO2008132313A3 (fr) | 2009-01-08 |
Family
ID=38630463
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/FR2008/000293 WO2008132313A2 (fr) | 2007-03-30 | 2008-03-05 | Réacteur échangeur compact utilisant une pluralité de brûleurs poreux |
Country Status (8)
Country | Link |
---|---|
US (1) | US8834586B2 (fr) |
EP (1) | EP2132486B1 (fr) |
JP (1) | JP5298118B2 (fr) |
KR (1) | KR101426979B1 (fr) |
CA (1) | CA2679528C (fr) |
FR (1) | FR2914395B1 (fr) |
RU (1) | RU2459172C2 (fr) |
WO (1) | WO2008132313A2 (fr) |
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US8133445B2 (en) | 2008-10-07 | 2012-03-13 | IFP Energies Nouvelles | Reaction chamber promoting heat exchange between the reagents and the gases that are produced |
RU2598435C2 (ru) * | 2011-08-26 | 2016-09-27 | Ифп Энержи Нувелль | Теплообменный реактор для производства водорода с помощью встроенного пучка парогенератора |
RU207959U1 (ru) * | 2021-05-21 | 2021-11-26 | Антон Сергеевич Пашкин | Быстропроточный термохимический реактор высокого давления |
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DE102009039276A1 (de) * | 2009-08-28 | 2011-03-10 | Bekon Energy Technologies Gmbh & Co. Kg | Reaktormodul für endotherme Reaktionen sowie Reaktor mit einer Mehrzahl von solchen Reaktormodulen |
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ITRM20110176A1 (it) * | 2011-04-07 | 2012-10-08 | Francesco Giacobbe | "perfezionamento nei reattori catalitici per reazioni endotermiche, in particolare per la produzione di idrogeno e gas di sintesi" |
FR3020968B1 (fr) * | 2014-05-16 | 2016-05-13 | Ifp Energies Now | Reacteur a lit radial multitubulaire |
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GB201813431D0 (en) * | 2018-08-17 | 2018-10-03 | Weedon Geoffrey Gerald | Process & apparatus for steam reforming |
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CN110575792A (zh) * | 2019-08-26 | 2019-12-17 | 清华大学 | 一种换热式硫酸催化分解反应器及催化方法 |
CN115353909B (zh) * | 2022-08-17 | 2024-03-26 | 西安交通大学 | 一种超临界水多孔介质氢氧化放热反应器及其工作方法 |
Citations (9)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3119671A (en) * | 1960-09-28 | 1964-01-28 | Chemical Coustruction Corp | Upright fluid heating furnace with heat recovery system |
US4900245A (en) * | 1988-10-25 | 1990-02-13 | Solaronics | Infrared heater for fluid immersion apparatus |
EP0430804A1 (fr) * | 1989-12-01 | 1991-06-05 | Institut Français du Pétrole | Procédé et dispositif de production d'hydrocarbures à partir d'une charge d'hydrocarbures aliphatiques dans un réacteur chauffé par un lit fluidisé de particules |
EP0895806A2 (fr) * | 1993-06-16 | 1999-02-10 | The Standard Oil Company | Procédé pour effectuer des réactions endothermiques |
DE19905327A1 (de) * | 1998-09-04 | 2000-03-09 | Linde Ag | Verfahren und Primärreformer zur Erzeugung von Synthesegas |
DE19921420A1 (de) * | 1999-05-08 | 2000-11-16 | Krupp Uhde Gmbh | Primärreformer zum Einsatz bei der Methanol- oder Ammoniakgewinnung |
GB2359764A (en) * | 2000-03-01 | 2001-09-05 | Geoffrey Gerald Weedon | An endothermic tube reactor |
US6296814B1 (en) * | 1998-11-10 | 2001-10-02 | International Fuel Cells, L.L.C. | Hydrocarbon fuel gas reformer assembly for a fuel cell power plant |
EP1464910A2 (fr) * | 2003-04-04 | 2004-10-06 | Air Products And Chemicals, Inc. | Appareil et méthode pour empêcher la corrosion par effusement métallique |
Family Cites Families (11)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3449671A (en) * | 1966-02-18 | 1969-06-10 | Tektronix Inc | Oscillographic apparatus for measuring the magnitude and duration of input waveforms |
ZA911838B (en) * | 1990-04-03 | 1991-12-24 | Standard Oil Co Ohio | Endothermic reaction apparatus |
SU1745329A1 (ru) * | 1990-09-25 | 1992-07-07 | Ленинградский Технологический Институт Им.Ленсовета | Газожидкостный аппарат |
EP0834465B1 (fr) * | 1996-10-04 | 2000-07-19 | Haldor Topsoe A/S | Procédé de reformage à la vapeur |
AU4733199A (en) * | 1998-09-04 | 2000-03-16 | Linde Aktiengesellschaft | Process and primary reformer for generating synthesis gas |
JP2001009264A (ja) * | 1999-04-26 | 2001-01-16 | Toyo Eng Corp | 熱交換器様式反応器 |
US6497856B1 (en) * | 2000-08-21 | 2002-12-24 | H2Gen Innovations, Inc. | System for hydrogen generation through steam reforming of hydrocarbons and integrated chemical reactor for hydrogen production from hydrocarbons |
US7250151B2 (en) * | 2002-08-15 | 2007-07-31 | Velocys | Methods of conducting simultaneous endothermic and exothermic reactions |
JP3966831B2 (ja) * | 2003-04-21 | 2007-08-29 | 大阪瓦斯株式会社 | 改質装置用の加熱バーナ |
JP4477432B2 (ja) * | 2004-06-29 | 2010-06-09 | 東洋エンジニアリング株式会社 | 改質器 |
EP1791631A1 (fr) * | 2004-09-21 | 2007-06-06 | Worcester Polytechnic Institute | Reacteur et procede de reformage a la vapeur d'eau |
-
2007
- 2007-03-30 FR FR0702410A patent/FR2914395B1/fr not_active Expired - Fee Related
-
2008
- 2008-03-05 KR KR1020097019587A patent/KR101426979B1/ko active IP Right Grant
- 2008-03-05 US US12/593,510 patent/US8834586B2/en not_active Expired - Fee Related
- 2008-03-05 WO PCT/FR2008/000293 patent/WO2008132313A2/fr active Application Filing
- 2008-03-05 JP JP2010501548A patent/JP5298118B2/ja not_active Expired - Fee Related
- 2008-03-05 CA CA2679528A patent/CA2679528C/fr not_active Expired - Fee Related
- 2008-03-05 EP EP20080775633 patent/EP2132486B1/fr not_active Not-in-force
- 2008-03-05 RU RU2009140147/06A patent/RU2459172C2/ru not_active IP Right Cessation
Patent Citations (9)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3119671A (en) * | 1960-09-28 | 1964-01-28 | Chemical Coustruction Corp | Upright fluid heating furnace with heat recovery system |
US4900245A (en) * | 1988-10-25 | 1990-02-13 | Solaronics | Infrared heater for fluid immersion apparatus |
EP0430804A1 (fr) * | 1989-12-01 | 1991-06-05 | Institut Français du Pétrole | Procédé et dispositif de production d'hydrocarbures à partir d'une charge d'hydrocarbures aliphatiques dans un réacteur chauffé par un lit fluidisé de particules |
EP0895806A2 (fr) * | 1993-06-16 | 1999-02-10 | The Standard Oil Company | Procédé pour effectuer des réactions endothermiques |
DE19905327A1 (de) * | 1998-09-04 | 2000-03-09 | Linde Ag | Verfahren und Primärreformer zur Erzeugung von Synthesegas |
US6296814B1 (en) * | 1998-11-10 | 2001-10-02 | International Fuel Cells, L.L.C. | Hydrocarbon fuel gas reformer assembly for a fuel cell power plant |
DE19921420A1 (de) * | 1999-05-08 | 2000-11-16 | Krupp Uhde Gmbh | Primärreformer zum Einsatz bei der Methanol- oder Ammoniakgewinnung |
GB2359764A (en) * | 2000-03-01 | 2001-09-05 | Geoffrey Gerald Weedon | An endothermic tube reactor |
EP1464910A2 (fr) * | 2003-04-04 | 2004-10-06 | Air Products And Chemicals, Inc. | Appareil et méthode pour empêcher la corrosion par effusement métallique |
Cited By (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US8133445B2 (en) | 2008-10-07 | 2012-03-13 | IFP Energies Nouvelles | Reaction chamber promoting heat exchange between the reagents and the gases that are produced |
CN102211002A (zh) * | 2010-04-12 | 2011-10-12 | 中科合成油技术有限公司 | 一种热油循环和冷激式固定床费托合成反应器及其应用 |
CN102211002B (zh) * | 2010-04-12 | 2013-03-27 | 中科合成油技术有限公司 | 一种热油循环和冷激式固定床费托合成反应器及其应用 |
RU2598435C2 (ru) * | 2011-08-26 | 2016-09-27 | Ифп Энержи Нувелль | Теплообменный реактор для производства водорода с помощью встроенного пучка парогенератора |
RU207959U1 (ru) * | 2021-05-21 | 2021-11-26 | Антон Сергеевич Пашкин | Быстропроточный термохимический реактор высокого давления |
Also Published As
Publication number | Publication date |
---|---|
KR20090127887A (ko) | 2009-12-14 |
RU2009140147A (ru) | 2011-05-20 |
KR101426979B1 (ko) | 2014-08-06 |
CA2679528C (fr) | 2015-09-15 |
WO2008132313A3 (fr) | 2009-01-08 |
JP5298118B2 (ja) | 2013-09-25 |
EP2132486B1 (fr) | 2015-05-13 |
US20100189638A1 (en) | 2010-07-29 |
FR2914395B1 (fr) | 2009-11-20 |
FR2914395A1 (fr) | 2008-10-03 |
CA2679528A1 (fr) | 2008-11-06 |
US8834586B2 (en) | 2014-09-16 |
EP2132486A2 (fr) | 2009-12-16 |
JP2010524811A (ja) | 2010-07-22 |
RU2459172C2 (ru) | 2012-08-20 |
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