WO2019045444A1 - Réacteur de reformage modulaire - Google Patents

Réacteur de reformage modulaire Download PDF

Info

Publication number
WO2019045444A1
WO2019045444A1 PCT/KR2018/009982 KR2018009982W WO2019045444A1 WO 2019045444 A1 WO2019045444 A1 WO 2019045444A1 KR 2018009982 W KR2018009982 W KR 2018009982W WO 2019045444 A1 WO2019045444 A1 WO 2019045444A1
Authority
WO
WIPO (PCT)
Prior art keywords
tube
reaction tube
combustion
reforming
heat exchange
Prior art date
Application number
PCT/KR2018/009982
Other languages
English (en)
Korean (ko)
Inventor
김효식
김진호
정기진
오승천
홍범의
강석환
Original Assignee
고등기술연구원 연구조합
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by 고등기술연구원 연구조합 filed Critical 고등기술연구원 연구조합
Publication of WO2019045444A1 publication Critical patent/WO2019045444A1/fr

Links

Images

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
    • 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
    • B01J2208/06—Details of tube reactors containing solid particles
    • B01J2208/065—Heating or cooling the reactor
    • 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
    • C01B2203/0244—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being an autothermal reforming step, e.g. secondary reforming processes
    • 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
    • C01B2203/025—Processes for making hydrogen or synthesis gas containing a partial oxidation step
    • C01B2203/0261—Processes for making hydrogen or synthesis gas containing a partial oxidation step containing a catalytic partial oxidation step [CPO]
    • 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
    • C01B2203/0833—Heating by indirect heat exchange with hot fluids, other than combustion gases, product gases or non-combustive exothermic reaction product gases
    • 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
    • C01B2203/0838—Methods of heating the process for making hydrogen or synthesis gas by heat exchange with exothermic reactions, other than by combustion of fuel
    • 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 modular reforming reactor.
  • a hot combustion flue gas is supplied to the shell side using a shell & tube type multi-tube reactor, and the heat of the combustion flue gas is transferred to the reforming reactor through indirect heating.
  • the reforming reaction which is an endothermic reaction in the catalyst
  • the partial oxidation reaction which is an exothermic reaction
  • Preheating to a reaction temperature of about 700 ° C or more is essential, and the steam / carbon ratio (s / c ratio) of the reactant can not be kept high to maintain the reaction temperature.
  • the autothermal reforming reaction increases the s / c ratio in order to avoid the carbon deposition condition in the reforming reaction of aromatic hydrocarbons since the risk of carbon deposition increases as the hydrocarbon of the reactant increases under the low s / c ratio condition.
  • the embodiment of the present invention improves the energy efficiency of the entire system by using the waste heat of the syngas discharged after the reforming reaction for heat exchange and conducts the heat of the combustion reaction unit separately so that the local temperature decrease of the reformer, And to provide a modular reforming reactor capable of preventing the reaction.
  • a tube module An upper cover installed on an upper portion of the tube module; And a lower cover installed at a lower portion of the tube module, wherein the tube module includes a reforming reaction tube charged with a reforming catalyst therein and generating a syngas by reaction of reactants supplied from the outside with the reforming catalyst; A heat exchange tube which receives the synthesis gas from the reforming reaction tube and transfers the waste heat of the supplied synthesis gas to the reforming reaction tube; And a combustion catalyst is charged into the inside of the reforming tube, the synthesis gas is supplied from the heat exchange tube, a combustion gas is generated by reaction of the fuel supplied from the outside with the combustion catalyst, And a combustion reaction tube for delivering the mixed gas, which is mixed with the combustion gas and the syngas, to a lower portion of the reaction tube.
  • the tube module includes a reforming reaction tube charged with a reforming catalyst therein and generating a syngas by reaction of reactants supplied from the outside with the reforming catalyst; A heat exchange tube which receives the synthesis gas from the reforming reaction tube
  • the heat exchange tube and the combustion reaction tube may communicate with each other at an upper end, and the reforming reaction tube and the heat exchange tube may communicate with each other at a lower end.
  • the lower cover may include a gas outlet for discharging the mixed gas discharged from the combustion reaction tube to the outside.
  • the reforming reaction tube is formed along the longitudinal direction of the tube module at the center of the tube module, and a plurality of the heat exchange tubes are formed to be spaced apart from each other in the circumferential direction about the reforming reaction tube, A plurality of the heat exchange tubes may be disposed between the plurality of heat exchange tubes along the circumferential direction about the reforming reaction tube.
  • the reforming reaction tube, the heat exchange tube, and the combustion reaction tube may each have a hexagonal cross-sectional structure.
  • the upper portion of the reforming reaction tube may be formed so as to protrude from the upper portion of the tube module more than the heat exchange tube and the combustion reaction tube.
  • the upper end of the inner partition wall formed at the interface between the heat exchange tube and the combustion reaction tube at an upper portion of the tube module is positioned at a lower position than the upper end of the outer tube portion of the tube module so that the synthesis gas is transferred from the heat exchange tube to the combustion reaction tube .
  • the upper cover may be coupled to an upper end of the outer frame of the tube module, and a through hole may be formed at the center of the upper cover to allow the upper portion of the reforming reaction tube to pass airtightly.
  • the upper cover may be provided with a fuel inlet for supplying fuel and air to the combustion reaction tube.
  • a lower end of an inner partition wall formed at an interface between the reforming reaction tube and the heat exchange tube at a lower portion of the tube module is connected to the outer periphery of the tube module and the outer tube of the tube module so that the syngas is transferred from the reforming reaction tube to the heat exchange tube. And may be formed at a position higher than the lower end of the other inner wall.
  • the lower cover further includes: a body; A separation plate disposed at an upper portion of the body and closely attached to a lower end of an outer frame of the tube module; A center support part supported at a center of the separator plate and inserted into an end of the reforming reaction tube to support the reforming catalyst and to allow the synthesis gas to pass therethrough; A side support part installed at an edge of the separator plate corresponding to the combustion reaction tube and inserted into an end of the combustion reaction tube to support the combustion catalyst and to pass the mixed gas; And a gas outlet provided on one side of the body for discharging the mixed gas having passed through the side support to the outside.
  • fine pores through which gas can pass may be formed in the center support portion and the side support portion.
  • the waste heat of the syngas discharged after the reforming reaction is used for heat exchange to improve the energy efficiency of the entire system, and the heat of the combustion reaction tube separately provided is transferred to the reforming reaction tube, Together, the local temperature drop of the reforming reaction tube can be prevented.
  • FIG. 1 is an external perspective view of a modular reforming reactor according to an embodiment of the present invention
  • FIG. 2A is an exploded perspective view showing the upper part of the tube module shown in FIG. 1,
  • FIG. 2B is a plan view of the " A " portion of FIG.
  • FIG. 3 is an exploded perspective view of FIG.
  • FIG. 4 is an exploded perspective view showing a lower portion of the tube module shown in FIG. 1,
  • FIG. 5A is an exploded perspective view of FIG. 4,
  • 5B is a bottom view of the portion " B " of Fig. 5A,
  • FIG. 6 is an explanatory view showing a gas flow in a modular reforming reactor according to an embodiment of the present invention.
  • FIG. 7 is a reference view showing the gas flow path on the top of the tube module in FIG. 6;
  • FIG. 8 is a reference view showing the gas flow path under the tube module in Fig.
  • a modular reforming reactor 10 may include a tube module 100, an upper cover 200, and a lower cover 300 have.
  • the tube module 100 is an element constituting most of the outer appearance of the modular reforming reactor 10 according to the present invention and may be formed into a substantially polygonal columnar shape.
  • the tube module 100 includes a reforming reaction tube 110, a heat exchange tube 120, and a combustion reaction tube 130 (as shown in FIGS. 2A, 2B, 3, 4, 5A, ).
  • one reforming reaction tube 110 may be formed at the center of the tube module 100, and a plurality of heat exchange tubes 120 and combustion reaction tubes 130 may be provided to center the reforming reaction tube 110 And may be alternately formed along the circumferential direction on the outer periphery thereof.
  • the arrangement of the reforming reaction tube 110, the heat exchange tube 120, and the combustion reaction tube 130 will be described in detail later.
  • the reforming reaction tube 110 can generate a syngas at a high temperature (about 800 ° C. or higher) by reacting with a reforming catalyst (not shown) charged in the reaction tube.
  • the reforming reaction tube 110 may be formed in a hexagonal column shape along the longitudinal direction of the tube module 100 at the center of the tube module 100 and may be formed as shown in FIGS.
  • the heat exchange tube 120 and the combustion reaction tube 130 may be formed to protrude above the tube module 100 as shown in FIG. Therefore, the upper portion of the reforming reaction tube 110 may protrude to the outside of the upper cover 200 through the upper cover 200.
  • the heat exchange tube 120 is configured to supply the high-temperature synthesis gas discharged from the reforming reaction tube 110 to the lower portion of the tube module 100 and to transfer the waste heat of the synthesis gas to the reforming reaction tube 110
  • the heat exchange tube 120 can transfer the waste heat of the synthesis gas to the reforming reaction tube 110 while moving the synthesis gas supplied from the lower part of the tube module 100 in the upward direction, Can be reheated by waste heat.
  • Combustion reaction tube 130 may be provided with syngas from heat exchange tube 120. Also, the combustion reaction tube 130 is provided with a separate fuel and air (oxygen) from the outside, and a reaction heat is generated by a partial oxidation reaction with a combustion catalyst (not shown) charged in the combustion reaction tube 130, Combustion gas can be produced as a product.
  • a separate fuel and air (oxygen) from the outside, and a reaction heat is generated by a partial oxidation reaction with a combustion catalyst (not shown) charged in the combustion reaction tube 130, Combustion gas can be produced as a product.
  • the reaction heat generated in the combustion reaction tube 130 is transferred to the reforming reaction tube 110 to raise the temperature of the reforming reaction tube 110 and the combustion gas is mixed with the synthesis gas provided in the upper part of the combustion reaction tube 130, And is moved downward of the reaction tube 130.
  • the reforming reaction tube 110 since the reforming reaction tube 110, the heat exchange tube 120, and the combustion reaction tube 130 each have a hexagonal cross-sectional structure, the reforming reaction tube 110 can be structured to have no gap therebetween, Efficiency can be maximized.
  • the heat exchange tube 120 is spaced from the center of the tube module 100 in the circumferential direction around the reforming reaction tube 110 formed along the longitudinal direction of the tube module 100, 130 may also be disposed between the heat exchange tubes 120 and spaced apart from each other around the reforming reaction tube 110 in the circumferential direction. Accordingly, the reforming reaction tube 110, the heat exchange tube 120, and the combustion reaction tube 130 may have the arrangement structure shown in the circle of FIG. 2B.
  • the heat exchange tube 120 is connected to the combustion reaction tube 130 so that the synthesis gas traveling along the heat exchange tube 120 can be transferred from the upper portion of the tube module 100 to the combustion reaction tube 130,
  • the upper end of the inner partition wall 121 formed at the interface of the reaction tube 130 may be formed lower than the upper end of the outer frame portion of the tube module 100.
  • the synthesis gas discharged from the upper portion of the heat exchange tube 120 is clogged by the upper cover 200 and can not flow out of the tube module 100 or enter the reforming reaction tube 110, Can be supplied to the upper portion of the combustion reaction tube 130 through a gap formed between the inner partition wall 121 and the upper cover 200 between the combustion reaction tubes 130.
  • the upper cover 200 is an element installed on the upper part of the tube module 100 and contacts the upper end of the outer frame of the tube module 100, that is, the upper end of the outer tube of the combustion reaction tube 130, So that the heat exchange tube 120 and the combustion reaction tube 130 are communicated with each other so that the syngas of the heat exchange tube 120 is supplied to the combustion reaction tube 130 as described above.
  • the top cover 200 may be coupled to the outer perimeter of the tube module 100 (specifically, the heat exchange tube 120 and the combustion reaction tube 130) And a through hole 201 through which the upper portion of the reforming reaction tube 110 protruding more than other tubes is airtightly inserted can be formed at the center of the upper cover 200.
  • the through holes 201 may be formed in a hexagonal shape corresponding to the size and shape of the reforming reaction tube 110.
  • the upper cover 200 may be provided with a fuel injection port 210 for supplying fuel and air (oxygen) to the combustion reaction tube 130.
  • the fuel injection port 210 may be a hollow pipe type in which the fuel and the air are moved. The fuel and air are supplied from the outside through the fuel injection port 210 to the combustion reaction tube 130 through the upper cover 200 .
  • the length of the lower end of the fuel injection port 210 may be set so as to be positioned directly above the combustion catalyst inserted into the combustion reaction tube 130.
  • a partial oxidation reaction may occur at the upper part of the combustion catalyst inserted in the combustion chamber 130, and reaction heat may be generated.
  • the combustion gas which is a product after the reaction, may be a mixed gas mixed with the synthesis gas and may be discharged to the lower portion of the combustion reaction tube 130.
  • the lower cover 300 is an element installed at a lower portion of the tube module 100.
  • the lower cover 300 is formed of a tube such that the reforming reaction tube 110 and the heat exchange tube 120 are connected to each other, And the synthesis gas of the reforming reaction tube 110 can be moved to the heat exchange tube 120 by being installed at a lower portion of the module 100.
  • the lower cover 300 may include a gas outlet 350 for discharging the mixed gas discharged from the combustion reaction tube 130 to the outside.
  • the structure of the reforming reaction tube 110, the heat exchange tube 120 and the combustion reaction tube 130 at the lower portion of the tube module 100 will be described in detail.
  • the position of the lower end of the inner partition 122 formed in the tube module 100 is such that the syngas is transferred from the reforming reaction tube 110 to the heat exchange tube 120 at the lower portion of the tube module 100, 100 may be formed to be higher than the position of the lower end of the other inner wall.
  • the heat exchanging tube 120 may be supplied to the heat exchanging tube 120 through a gap between the inner partition 122 and the lower cover 300 formed at the interface between the heat exchanging tube 120 and the heat exchanging tube 120, (See Fig. 8).
  • the lower cover 300 may include a body 310, a separation plate 320, a central support 330, a side support 340, and a gas outlet 350.
  • the body 310 is an element that forms the overall appearance of the lower cover 300 and can be installed or formed in another configuration.
  • the body 310 may have a substantially triangular structure, and each vertex of the triangular structure may be chamfered to form a plane.
  • the separator 320 is disposed on the upper portion of the body 310 and is closely attached to the lower end of the lower outer frame of the tube module 100 to prevent the outflow of various gases.
  • the central support part 330 is supported at a predetermined distance from the bottom of the separation plate 320 at the center of the separation plate 320.
  • the center support part 330 is inserted into the lower end of the reforming reaction tube 110, It is possible to support the reforming catalyst charged in the reforming catalyst 110.
  • the center support part 330 is separated from the bottom of the separator plate 320 and separated from the separator plate 320 through a central support plate 331.
  • the center support part 330 supports the reforming catalyst in the lower part to prevent the outflow of the reforming catalyst, h) may be formed to allow the synthesis gas to pass therethrough.
  • the side support part 340 may be installed at the edge of the separation plate 320 so as to be installed at a position corresponding to the combustion reaction tube 130.
  • the side support portion 340 may be inserted into the lower end of the combustion reaction tube 130 to support the combustion catalyst loaded in the combustion reaction tube 130.
  • the side support portion 340 may support the combustion catalyst at the lower portion to allow the mixed gas to pass while blocking the outflow of the combustion catalyst.
  • the gas discharge port 350 is provided on one side of the body 310 and the gas discharge port 350 is formed inside the body 310 so that the mixed gas passing through the side support portion 340 is discharged to the outside of the lower cover 300 And may be formed to communicate with the side support portion 340 and protrude to the outside of the body 310.
  • a reactant for example, a reforming reaction gas
  • the reactant is contacted with the reforming catalyst at a temperature of 700 ° C. or higher, .
  • the generated syngas passes through the central support portion 330 and is discharged to the lower portion of the reforming reaction tube 110 and is blocked by the separating plate 320 to form a plurality of (for example, three) heat exchange tubes 120). ≪ / RTI > The syngas introduced into the heat exchange tube 120 moves upward to heat the reforming reaction tube 110 and the combustion reaction tube 130 in contact with the heat exchange tube 120 to heat the tubes.
  • the syngas which has been moved upward through the heat exchange tube 120 can be moved to the combustion reaction tube 130 located next to the top of the tube module 100 as shown in FIG. 7, May be supplied to the combustion reaction tube (130).
  • the combustion reaction tube 130 generates a reaction heat as a partial oxidation reaction occurs between the fuel supplied from the outside through the fuel injection port 210 and the combustion catalyst loaded in the inside thereof.
  • the reaction heat may be transferred to the reforming reaction tube 110 to heat the reforming reaction tube 110.
  • the combustion gas which is a product of the combustion reaction, is mixed with the synthesis gas supplied to the upper portion of the combustion reaction tube 130 to become a mixture gas.
  • the mixture gas moves downward along the combustion reaction tube 130, 340 and may be discharged to the outside of the lower cover 300 through the gas outlet 350.
  • a gas flow is generated in which all of the synthesis gas flows from the lower side to the upper side.
  • the cocurrent flow in the heat exchange tube 120 causes the gas flow in the combustion reaction tube 130 to be directed downward do.
  • the fluid flow of the reforming reaction tube 110 and the combustion reaction tube 130 can be both flowing from the upper side to the lower side.
  • This co-current flow allows both the reforming catalyst and the combustion catalyst to meet at the top of the reactant, thereby closely matching the catalyst bed maximum active area height.
  • the endothermic reaction occurs in the reforming catalyst and the exothermic reaction occurs in the combustion catalyst when the upper portion of the catalyst layer, which is the most active part of each catalyst, is observed, so that localized heat supply can be performed above the reforming catalyst layer where the temperature decrease is concentrated.

Landscapes

  • 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)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)

Abstract

L'invention concerne un réacteur de reformage modulaire comprenant : un module de tube ; un couvercle supérieur installé au-dessus du module de tube et fermant une extrémité supérieure du module de tube ; et un couvercle inférieur installé sous le module de tube. Le module de tube comprend : un tube de réaction de reformage dans lequel un catalyseur de reformage est chargé et qui génère un gaz synthétisé par la réaction d'un réactif provenant de l'extérieur et du catalyseur de reformage ; un tube d'échange de chaleur qui reçoit le gaz synthétisé à partir du tube de réaction de reformage et transmet la chaleur perdue du gaz synthétisé reçu au tube de réaction de reformage ; et un tube de réaction de combustion dans lequel est chargé un catalyseur de combustion et qui reçoit le gaz synthétisé à partir du tube d'échange de chaleur, génère un gaz de combustion par la réaction d'un combustible provenant de l'extérieur et du catalyseur de combustion, transmet la chaleur du gaz de combustion généré au tube de réaction de reformage et décharge vers le bas un gaz mixte dans lequel le gaz de combustion et le gaz de synthèse sont mélangés.
PCT/KR2018/009982 2017-08-30 2018-08-29 Réacteur de reformage modulaire WO2019045444A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
KR10-2017-0110232 2017-08-30
KR1020170110232A KR101929012B1 (ko) 2017-08-30 2017-08-30 모듈형 개질 반응기

Publications (1)

Publication Number Publication Date
WO2019045444A1 true WO2019045444A1 (fr) 2019-03-07

Family

ID=64671252

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/KR2018/009982 WO2019045444A1 (fr) 2017-08-30 2018-08-29 Réacteur de reformage modulaire

Country Status (2)

Country Link
KR (1) KR101929012B1 (fr)
WO (1) WO2019045444A1 (fr)

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP3069743B2 (ja) * 1990-10-09 2000-07-24 溶融炭酸塩型燃料電池発電システム技術研究組合 燃料電池用二段触媒燃焼型改質器
JP2005255476A (ja) * 2004-03-12 2005-09-22 Toshiba Corp セラミック膜式合成ガス反応装置およびその運転方法
KR100818592B1 (ko) * 2006-11-30 2008-04-01 한국에너지기술연구원 촉매연소를 이용한 열 공급용 발열반응과 수소생산용흡열반응이 동시에 가능한 모듈타입 일체형 수소 리포머장치
KR20100071517A (ko) * 2008-12-19 2010-06-29 삼성에스디아이 주식회사 개질장치
JP2013229144A (ja) * 2012-04-24 2013-11-07 Honda Motor Co Ltd 燃料電池モジュール

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP3069743B2 (ja) * 1990-10-09 2000-07-24 溶融炭酸塩型燃料電池発電システム技術研究組合 燃料電池用二段触媒燃焼型改質器
JP2005255476A (ja) * 2004-03-12 2005-09-22 Toshiba Corp セラミック膜式合成ガス反応装置およびその運転方法
KR100818592B1 (ko) * 2006-11-30 2008-04-01 한국에너지기술연구원 촉매연소를 이용한 열 공급용 발열반응과 수소생산용흡열반응이 동시에 가능한 모듈타입 일체형 수소 리포머장치
KR20100071517A (ko) * 2008-12-19 2010-06-29 삼성에스디아이 주식회사 개질장치
JP2013229144A (ja) * 2012-04-24 2013-11-07 Honda Motor Co Ltd 燃料電池モジュール

Also Published As

Publication number Publication date
KR101929012B1 (ko) 2018-12-13

Similar Documents

Publication Publication Date Title
JPH0422827Y2 (fr)
JPH0522641B2 (fr)
CA2287288C (fr) Ensemble de recuperation des gaz de combustion d'un bruleur destine a un reformeur catalytique
US7297169B2 (en) Apparatus and method for hydrocarbon reforming process
CN108404821B (zh) 一种节能型高效径向甲醇反应器
WO2010005165A2 (fr) Dispositif de transformation du combustible d’un système de pile à combustible
CN101798086A (zh) 三氯硅烷制造装置以及三氯硅烷制造方法
JP4842805B2 (ja) マルチチャネルモノリシック構造のチャネルに出入りするよう２つの流体を分配する方法及び装置、並びにそれらの使用
WO2016167461A1 (fr) Appareil de génération de vapeur et système de pile à combustible comprenant ce dernier
GB1065044A (en) Catalytic reaction
ES2954324T3 (es) Reactor de conversión y guía de procedimiento
WO2019045444A1 (fr) Réacteur de reformage modulaire
CN111511463B (zh) 绝热轴向流动转化器
US10329159B2 (en) Axial-radial flow converter
WO2019066207A1 (fr) Boîtier de pile à combustible à double structure et système de pile à combustible l'utilisant
CN205235936U (zh) 一种组合式固定床反应器及由其形成的装置
WO2011034249A1 (fr) Appareil de refroidissement à étages séparables permettant d'éliminer la chaleur de réaction d'un réacteur ft à colonne à barbotage pour suspension
WO2010079922A2 (fr) Générateur de vapeur pour pile à combustible avec double utilisation pour chauffer le gaz de l'électrode à combustible
CN108722339B (zh) 径向气冷反应器
WO2019151567A1 (fr) Dispositif d'échange de chaleur
KR20030045965A (ko) 연료전지용 연료개질기
JPS6227305A (ja) プレ−ト形改質装置
CN211274586U (zh) 一种等温同壳多级反应装置
CN215963489U (zh) 一种水冷气冷组合式等温变换反应器
SU1058487A3 (ru) Реактор дл проведени гетерогенного катализа реакций газообразных реагентов под давлением

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 18851891

Country of ref document: EP

Kind code of ref document: A1

NENP Non-entry into the national phase

Ref country code: DE

122 Ep: pct application non-entry in european phase

Ref document number: 18851891

Country of ref document: EP

Kind code of ref document: A1