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WO2011134630A1 - Échangeur de chaleur pour le chauffage et le refroidissement rapides de fluides - Google Patents

Échangeur de chaleur pour le chauffage et le refroidissement rapides de fluides Download PDF

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Publication number
WO2011134630A1
WO2011134630A1 PCT/EP2011/002045 EP2011002045W WO2011134630A1 WO 2011134630 A1 WO2011134630 A1 WO 2011134630A1 EP 2011002045 W EP2011002045 W EP 2011002045W WO 2011134630 A1 WO2011134630 A1 WO 2011134630A1
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WO
WIPO (PCT)
Prior art keywords
section
heating
fluid
heat exchanger
cooling
Prior art date
Legal status (The legal status 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 status listed.)
Ceased
Application number
PCT/EP2011/002045
Other languages
German (de)
English (en)
Inventor
Klaus Schubert
Peter Pfeifer
Manfred Kraut
Roland Dittmeyer
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Karlsruher Institut fuer Technologie KIT
Original Assignee
Karlsruher Institut fuer Technologie KIT
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 Karlsruher Institut fuer Technologie KIT filed Critical Karlsruher Institut fuer Technologie KIT
Priority to EP11716488A priority Critical patent/EP2564143A1/fr
Publication of WO2011134630A1 publication Critical patent/WO2011134630A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D9/00—Heat-exchange apparatus having stationary plate-like or laminated conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F3/00—Plate-like or laminated elements; Assemblies of plate-like or laminated elements
    • F28F3/02—Elements or assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with recesses, with corrugations
    • F28F3/04—Elements or assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with recesses, with corrugations the means being integral with the element
    • F28F3/048—Elements or assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with recesses, with corrugations the means being integral with the element in the form of ribs integral with the element or local variations in thickness of the element, e.g. grooves, microchannels
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F2260/00—Heat exchangers or heat exchange elements having special size, e.g. microstructures
    • F28F2260/02—Heat exchangers or heat exchange elements having special size, e.g. microstructures having microchannels

Definitions

  • the invention relates to a heat exchanger system, preferably a microstructured heat exchanger system and a method for rapid heating and cooling of fluids, preferably liquids according to the first and tenth patent claim.
  • heat exchanger systems of the type mentioned above, fluid mixtures are rapidly heated to a specific temperature, kept at this temperature for a certain period of time, and then rapidly cooled again in the same system.
  • the fluid or the fluid mixture passes through a plurality of heat exchangers or heat exchanger areas in one or more fluid passages in the heat exchanger system serially, preferably continuously by means of a continuous fluid flow.
  • Such heat exchanger systems serve, for example, the sterilization of fluids, the controlled performance of chemical reactions or catalytic decomposition reactions.
  • a well-known version of a heat exchanger system comprises a plurality of separate heat exchangers and reaction chambers arranged one behind the other, which are each provided for a partial step (heating, reaction, cooling).
  • EP 1 162 888 B1 describes, by way of example, a method for killing harmful microorganisms in liquids by briefly heating to above 140 ° C. and subsequent cooling when using two serially connected microstructured crossflow heat exchangers. For optional maintenance of an isothermal hold time between heating and cooling, the use of a third intermediate heat exchanger is suggested.
  • the latter embodiment can be limited to a heat exchanger system of the type mentioned transferred. While two heaters are fundamentally similar in their temperature range and can also be arranged functionally next to one another in a microstructure apparatus, the integration of a heating and a cooling device in a common microstructure body inevitably leads to increased heat losses due to the short heat transfer paths without further heat-insulating measures. The efficiency is reduced accordingly with an increase in heat losses.
  • the object of the invention is to propose a further improved heat exchanger system and method for heating and cooling a fluid with an increased efficiency.
  • a heat exchanger and a method for rapid heating and cooling of a fluid in which the fluid is passed through at least one microchannel and heated and cooled therein.
  • the fluid in the microchannels is maintained at a temperature level between heating and cooling for a certain time (dwell time).
  • the temperature level is ideally defined by a target temperature, but in practice defined by a temperature interval between a lower and an upper dwell time.
  • the temperature span extends preferably ⁇ 5%, more preferably ⁇ 2% of the target temperature in ° C, preferably around this target temperature.
  • the fluid passes through a heating section for heating, a cooling section for cooling, and a residence time section therebetween.
  • the residence time zone comprises at least one area in which the fluid is converted from a heating into a cooling, preferably the area in which the fluid assumes the aforementioned temperature level or temperature interval.
  • the fluid passes through the heat exchanger as a fluid stream, preferably as a continuous fluid stream, more preferably - as designed - as a stationary fluid stream.
  • the method for rapidly heating and cooling a fluid in at least one microchannel comprises heating the fluid in a heating path (first step). Subsequently, in a second step, a forwarding of the fluid in a residence time with the same temperature or the aforementioned temperature level or temperature interval, followed by an introduction and cooling of the fluid in the cooling section (third step).
  • the residence time section preferably only the residence time section, has power supply means, preferably heating means. They not only determine the temperature level in the residence time, but also compensate for the heat losses in the aforementioned process, in particular the heating and cooling.
  • the heating means preferably comprise fluid guides for receiving and / or passing one or more tempering fluids on or around the microchannels in the region of Residence time distance.
  • tempering fluid serve liquid and gaseous fluids, preferably thermal oils, salt and metal melts or gases.
  • the fluid guides inside, in particular in the region of the microchannels of the residence time section, with a catalyst which triggers a chemical catalytic reaction with heat development (exothermic reaction) in the tempering fluid and selectively enables heating of the residence time section or a part thereof.
  • the fluid guides in particular the catalyst-coated fluid guide sections as reaction chamber with extended cross section and / or with an enlarged surface for the heat transfer (eg heating or cooling fins ) to design.
  • the reaction space can also be designed as a reaction mixing chamber with a merging and again bifurcation of a plurality of fluid guides.
  • Another embodiment provides electric heating cartridges or heating elements as heating means, which are used or integrated near the residence time in the heat exchanger.
  • both the tempering fluids as mixing additives or as reactants can be mixed into the fluids in the microchannels as well as any gases or vapors from evaporation or decomposition in the fluid can be diverted from the microchannels into the fluid channels, preferably aspirated.
  • the driving force for the Eimischung or suction is the pressure difference between the fluid in the
  • a preferred embodiment provides a membrane, preferably a selectively gas-permeable membrane (for the selective removal of gases) between microchannels and fluid channels.
  • the heating section comprises, if a process is carried out with a heating with a vapor or gas formation, an evaporator section and optionally an overheating section, the cooling section a Condensation section. If the fluid to be heated enters the heating section in a vapor or gaseous state, the heating-up section only consists of an overheating section.
  • a plurality of parallel-connected microchannels are provided, further preferably in the heat exchanger bundle parallel to each other.
  • the parallel-connected microchannels further preferably have the same geometric dimensions.
  • a further embodiment provides that the microchannels of the heating section and / or the cooling section have at least one intermediate volume into which all or one of the microchannels of the heating section and / or the cooling section terminate and exit again.
  • Several preferably similar intermediate volumes with preferably an equal number of inflowing and outflowing microchannels (microchannel groups) can be arranged parallel to one another and thus form a voluminous group. Mixing of the microchannel groups with each other is in turn realized by a second, the first downstream Voluminalui of mutually parallel intermediate volumes, which are arranged offset with respect to the previous intermediate volumes, i. span from these deviating microchannel groups.
  • the intermediate volume or volumes serve to intermix fluid flow from the microchannels during heating or cooling, particularly to reduce material and thermal inhomogeneities, and thus, e.g. of premature local evaporation.
  • the intermediate volumes may also be provided with inlets or outlets for admixtures of additional fluids and / or selective aspirations, e.g. of gases - as otherwise described in the other context - use.
  • the residence time range can be used and designed as a reaction volume or a plurality of reaction volumes arranged in parallel for a chemical reaction. It is within the scope of further embodiments of the invention to design the power supply means not as a heating means, but as a coolant, wherein the fluid to be treated is first introduced into the cooling section and cooled, then in the residence time a temperature minimum passes, then reheated in the heating to become. As described above, the heating path and the cooling section are thermally connected to each other.
  • FIG. 1 shows an embodiment of a micro heat exchanger with countercurrent heat exchange element
  • FIG. 2 shows an embodiment of a micro-heat exchanger with cross-flow heat exchanger element
  • FIG. 1 shows an embodiment of a micro heat exchanger with countercurrent heat exchange element and a power segregation by catalytic reaction
  • FIG. 5 shows a single film of a micro heat exchanger with grooved incorporated fluid guides for a heating line
  • FIG. 6 shows a schematic representation of the process sequence for the production of hydrogen cyanide from formamide.
  • a heat exchanger of the aforementioned type as disclosed in FIGS. 1 and 2 in a respective sectional view, comprises at least one microchannel 1 with a heating section 2, a residence section 3 and a cooling section 4, wherein the heating section and the cooling section are thermally connected to each other and the residence time section has power supply means 5.
  • the microchannels are flowed through by a fluid idstrom, wherein the flow direction 9 is indicated by arrows.
  • the fluid flow is in the supply 10, that is, before entry into the heating section 2, a starting temperature e i n and leaves the cooling coil from having an exit temperature T.
  • Fig.l shows an embodiment in which the heating section 2 and cooling section 4 are flowed through in countercurrent to each other (countercurrent heat exchange element).
  • the extent of the heating and the cooling and thus the countercurrent heat exchange element, but also the residence time 3 in the heat exchanger is represented by dimension arrows and dashed lines.
  • the part of the residence time section facing the aforementioned countercurrent heat exchange element is the power input path 8, which is preferably equipped with larger and / or more strongly dimensioned power supply means 5 compared to the remaining area of the residence time section.
  • These reinforced power supply means serve in addition to the temperature of the power input point and the thermal buffering between heating / cooling and the remaining residence time and also to compensate for heat losses in the heat exchanger, in particular caused by the temperature difference between the starting temperature e in and the outlet temperature T out . If appropriate, endothermic or exothermic reactions taking place in the fluid flow or inlets or outlets of partial flows in the fluid flow must be taken into account in the heat exchanger, in particular in the dwelling time zone.
  • the heating sections 2 and cooling sections 4 are flowed through in cross-flow to each other (cross-flow heat exchange element).
  • the extent of the cooling sections 4 comprises only a partial area 12 of the heating-up section, which in this exemplary embodiment has additional inlet cooling channels 13 and heat-insulating cavities 11.
  • the inlet cooling channels are used for tion of a coolant and thus the regulation of the inlet temperature e in the fluid flow, while the heat-insulating cavities 11 reduce the action of the coolant in the portion 12.
  • Fig.l to 6 show examples of embodiments of Mikroärmetausehern.
  • the illustrated variants comprise at least one heat exchanger of the aforementioned type, wherein the microchannels 1 are integrated as groove-shaped incorporated fluid guides and the power supply means 5 in sheets 6 (individual sheets) of a film stack. Breakthroughs 7 serve as fluid guide connections between two microchannels. The thermal connection between the heating and cooling path takes place via the remaining film section between the microchannels.
  • the two superimposed and one-sided structured films in FIGS. 1 to 4 with the heating section 2 and the cooling section 4 can be replaced by a film structured on both sides, the heating section 2 being incorporated on one side of the film and the cooling section 4 being incorporated on the other side ,
  • the residence time section comprises a tion insertion 8, which preferably (but not shown) has a higher density of cartridge heaters or more powerful cartridge heaters to compensate for losses in particular from the areas of the heating sections 2 and 4 cooling lines.
  • the heating cartridges are used in at least one film, preferably in separate films in holes 14, alternatively in recesses or in ril- lenförmigen cavities. A slight interference fit with optional thermal paste between the inner wall of the holes and the cartridge heaters used promotes heat input in an advantageous manner.
  • FIG. 4 exemplarily represents a design with a power input through chemical reactions, preferably catalytic reactions with heat development.
  • the power supply means are arranged in the region of the residence time section 3, more preferably in the power input section 8. They include fluid guides 16, in which a reactive gas, such as preferably CH 4 or H 2, is introduced into the heat exchanger and from there is sprayed into a gas channel 18, preferably flat, through injection openings 17.
  • a reactive gas such as preferably CH 4 or H 2
  • the gas channel is traversed by an oxygen-containing gas, preferably air, in particular in the region of the power input path 8 to a reaction in the example for the exothermic reaction of oxygen 0 2 with hydrogen H 2 or hydrocarbon CH 4 comes.
  • the gas channel is preferably coated with a catalyst for reaction control and / or concentration, more preferably in the region of the power input section 8 or the residence time section 3.
  • the gas flow 19 heated by the reaction preferably transfers heat in countercurrent directly to the fluid flow in the channels 1, Preferably, as shown in the example, first on the residence time section 3 and then also on the heating 2.
  • An effective heat transfer is achieved by a thin membrane 20 between the gas flow 19 and fluid flow (flow direction 9).
  • the cooling section 4 is preferably thermally insulated from the gas flow and preferably has an increased heat conductivity selectively acting on the heating section. The heat from the cooling section is preferred on the Heating the fluid flows used in the heating sections and then does not escape into the gas flow.
  • An alternative embodiment provides a non-fluid-tight or selectively permeable membrane, which allows mass transfer between the fluid and the gas and can be used to generate and control reactions in the fluid flow.
  • the reactions on the gas side are preferably a selective oxidation, for example the partial oxidation of hydrocarbons to synthesis gas, the selective oxidation of CO in the presence of hydrogen, the production of hydrogen peroxide from hydrogen and oxygen in the Oxygen depletion, production of peroxide compounds (propene oxide, epoxybutene) or oxidative dehydrogenation of hydrocarbons such as propene.
  • a selective oxidation for example the partial oxidation of hydrocarbons to synthesis gas, the selective oxidation of CO in the presence of hydrogen, the production of hydrogen peroxide from hydrogen and oxygen in the Oxygen depletion, production of peroxide compounds (propene oxide, epoxybutene) or oxidative dehydrogenation of hydrocarbons such as propene.
  • a selective separation of individual reaction products such as hydrogen over the membrane 20; the resulting free reaction space is the reaction additionally available.
  • Selective removal of gases also allows adjustment of higher reaction pressures, exploiting the shift in thermodynamic equilibrium by removing the hydrogen; This results
  • the heating section 2 are preferably hydrogenations in the gas phase, such as nitrobenzene or toluene, or in ionic liquids, if their temperature stability allows a coupling with the oxidation reaction.
  • Endothermic reactions on said fluid side which do not require a membrane, are preferably surface-catalyzed decomposition reactions (methanol, propane, etc.) or reforming processes.
  • the coupling of a hydrogen-oxygen reaction to hydrogen peroxide on the gas side could also be connected via a non-selective membrane 20 with an epoxidation, wherein the product hydrogen peroxide would be useful as Epoxidmaschinesreagenz.
  • Heat exchangers in which the fluid is vaporized and preferably also recondensed preferably have correspondingly adapted evaporator sections and possibly cooling sections.
  • 5 shows by way of example in phantom top view of a sheet 6 with groove-shaped incorporated microchannels 1 in the region of the heating section 2 as well as the delay zone 3 with power input path 8.
  • the Auftropicstre ⁇ bridge comprises Besides one diesstechniksaufconcerank 23 as schematically shown an evaporation path 21 for the phase transition from liquid to vapor / gaseous and / or an overheating section 22 for further overheating of the steam or gas.
  • the essential design of these subregions, in particular the evaporator section takes into account the volume increase in the fluid flow when the microchannels flow through.
  • the liquid heating section and the superheat section in which idealized no changes in the physical state of the fluid take place, each have a constant cross section with a large specific surface area for rapid heat transfer.
  • the region in which a phase transition takes place with an increase in volume preferably the evaporator section, is characterized by a continuous increase in cross section of the microchannels in the flow direction (see FIG.
  • means for pressure equalization between the microchannels between the microchannels comprise either a fluidic connection such as passages between the
  • the intermediate volumes each bundle and connect a number of microchannels.
  • these can be connected in parallel to one another in each case for a bundle, wherein, in the context of a further embodiment, additional volumes cascaded and offset enable a fluidic connection of the bundles to one another.
  • a cooling section which is also to be used for a recondensation or a condensation, can in principle be made variable in its flow cross section as a function of the fluid composition in the flow direction. In this case, all the measures mentioned incl.
  • the cooling section 4 consists of three areas.
  • the residence time line 3 first opens into the gas cooling section 26, which is designed for the cooling of the gas or the vapor to the condensation temperature (boiling temperature). Ideally, but not necessarily in the real state, no condensation takes place here.
  • the microchannels open into the condensation section 25, which is designed for a complete condensation, ie a transfer of gaseous or vaporous constituents into liquid constituents and is designed to be tapered in its flow cross section, preferably adapted to a volume reduction.
  • the condensation section 25 downstream of the condensation section follows from further cooling of the present as a liquid fluid on T.
  • a volume change in a phase transition and / or a change in cross section of the microchannels can be used as an alternative or additional measure also for a change in the flow rate in the microchannels 1 in the flow direction 9 and thus the locally to be effected heat transfer between cooling and heating.
  • Fig. 6 schematically shows a continuous chemical process in a heat exchanger (preferably countercurrent circuit) of the aforementioned type again, in the example, the continuous production of isocyanate 28 is shown as the starting liquid liquid carbonate 27 (RN-CO-CH 3 ) as the input fluid. Carbonate is starting from ⁇ ⁇ _.
  • the residence time section serves as a reaction volume, depending on the desired temperature and reaction control as separate microchannels or as a common intermediate volume for microchannel bundles.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)

Abstract

L'invention concerne un échangeur de chaleur pour le chauffage et le refroidissement rapides d'un fluide dans au moins un microcanal (1), comprenant un parcours de chauffe (2), un parcours de temps de séjour (3) et un parcours de refroidissement (4). L'invention a pour but d'obtenir un système échangeur de chaleur amélioré, présentant un rendement élevé. A cet effet, l'échangeur de chaleur selon l'invention se caractérise en ce que le parcours de chauffe et le parcours de refroidissement interconnectés thermiquement et en ce que seul le parcours de temps de séjour présente des moyens d'apport de puissance (5).
PCT/EP2011/002045 2010-04-30 2011-04-21 Échangeur de chaleur pour le chauffage et le refroidissement rapides de fluides Ceased WO2011134630A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
EP11716488A EP2564143A1 (fr) 2010-04-30 2011-04-21 Échangeur de chaleur pour le chauffage et le refroidissement rapides de fluides

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102010018869.7 2010-04-30
DE201010018869 DE102010018869A1 (de) 2010-04-30 2010-04-30 Wärmetauscher zum schnellen Erhitzen und Abkühlen von Fluiden

Publications (1)

Publication Number Publication Date
WO2011134630A1 true WO2011134630A1 (fr) 2011-11-03

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PCT/EP2011/002045 Ceased WO2011134630A1 (fr) 2010-04-30 2011-04-21 Échangeur de chaleur pour le chauffage et le refroidissement rapides de fluides

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Country Link
EP (1) EP2564143A1 (fr)
DE (1) DE102010018869A1 (fr)
WO (1) WO2011134630A1 (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102015111614A1 (de) 2015-07-17 2017-01-19 Karlsruher Institut für Technologie Mikrostrukturreaktor zur Durchführung exothermer, heterogen katalysierter Reaktionen mit effizienter Verdampfungskühlung
WO2017211864A1 (fr) * 2016-06-07 2017-12-14 Karlsruher Institut für Technologie Microréacteur de méthanisation et mise en œuvre d'un procédé de méthanisation

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102021208923A1 (de) 2021-08-13 2023-02-16 Ineratec Gmbh Plattenelement für reaktionsmodule oder -systeme
DE102021210989A1 (de) 2021-09-30 2023-03-30 Siemens Mobility GmbH Thermische Desinfektionsvorrichtung

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5005640A (en) * 1989-06-05 1991-04-09 Mcdonnell Douglas Corporation Isothermal multi-passage cooler
US6200536B1 (en) * 1997-06-26 2001-03-13 Battelle Memorial Institute Active microchannel heat exchanger
EP1162888B1 (fr) 1999-03-19 2003-10-15 Forschungszentrum Karlsruhe GmbH Procede permettant de tuer les microorganismes nuisibles contenus dans des liquides par traitememt a haute temperature de courte duree
US20040199039A1 (en) * 2003-04-07 2004-10-07 Brophy John H. Dehydrogenation reactions in narrow reaction chambers and integrated reactors
DE202005013835U1 (de) * 2005-09-01 2005-11-10 Syntics Gmbh Vorrichtung zum schnellen Aufheizen, Abkühlen, Verdampfen oder Kondensieren von Fluiden
DE10132370B4 (de) 2001-07-04 2007-03-08 P21 - Power For The 21St Century Gmbh Vorrichtung und Verfahren zum Verdampfen flüssiger Medien

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE19608824A1 (de) * 1996-03-07 1997-09-18 Inst Mikrotechnik Mainz Gmbh Verfahren zur Herstellung von Mikrowärmetauschern
DE19825102C2 (de) * 1998-06-05 2001-09-27 Xcellsis Gmbh Verfahren zur Herstellung eines kompakten katalytischen Reaktors

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5005640A (en) * 1989-06-05 1991-04-09 Mcdonnell Douglas Corporation Isothermal multi-passage cooler
US6200536B1 (en) * 1997-06-26 2001-03-13 Battelle Memorial Institute Active microchannel heat exchanger
EP1162888B1 (fr) 1999-03-19 2003-10-15 Forschungszentrum Karlsruhe GmbH Procede permettant de tuer les microorganismes nuisibles contenus dans des liquides par traitememt a haute temperature de courte duree
DE10132370B4 (de) 2001-07-04 2007-03-08 P21 - Power For The 21St Century Gmbh Vorrichtung und Verfahren zum Verdampfen flüssiger Medien
US20040199039A1 (en) * 2003-04-07 2004-10-07 Brophy John H. Dehydrogenation reactions in narrow reaction chambers and integrated reactors
DE202005013835U1 (de) * 2005-09-01 2005-11-10 Syntics Gmbh Vorrichtung zum schnellen Aufheizen, Abkühlen, Verdampfen oder Kondensieren von Fluiden

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102015111614A1 (de) 2015-07-17 2017-01-19 Karlsruher Institut für Technologie Mikrostrukturreaktor zur Durchführung exothermer, heterogen katalysierter Reaktionen mit effizienter Verdampfungskühlung
WO2017013003A1 (fr) 2015-07-17 2017-01-26 Karlsruher Institut für Technologie Microréacteur structuré destiné à la conduite de réactions de catalyse hétérogène exothermiques avec un refroidissement par évaporation efficace
US10150093B2 (en) 2015-07-17 2018-12-11 Ineratec Gmbh Microstructure reactor for carrying out exothermic heterogenously-catalysed reactions with efficient evaporative cooling
WO2017211864A1 (fr) * 2016-06-07 2017-12-14 Karlsruher Institut für Technologie Microréacteur de méthanisation et mise en œuvre d'un procédé de méthanisation
US11229894B2 (en) 2016-06-07 2022-01-25 Karlsruher Institut Fuer Technologie Micro-reactor and method implementation for methanation

Also Published As

Publication number Publication date
EP2564143A1 (fr) 2013-03-06
DE102010018869A8 (de) 2012-06-14
DE102010018869A1 (de) 2011-11-03

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