EP1966559B1 - Unite d'echangeur de chaleur destinee a recuperer de la chaleur a partir d'un ecoulement de gaz chaud - Google Patents

Unite d'echangeur de chaleur destinee a recuperer de la chaleur a partir d'un ecoulement de gaz chaud Download PDF

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Publication number
EP1966559B1
EP1966559B1 EP06808029.0A EP06808029A EP1966559B1 EP 1966559 B1 EP1966559 B1 EP 1966559B1 EP 06808029 A EP06808029 A EP 06808029A EP 1966559 B1 EP1966559 B1 EP 1966559B1
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EP
European Patent Office
Prior art keywords
heat exchanger
flow
heat
gas
exchanger unit
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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.)
Not-in-force
Application number
EP06808029.0A
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German (de)
English (en)
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EP1966559A4 (fr
EP1966559A1 (fr
Inventor
Juha Huotari
Juha Honkatukia
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MW Power Oy
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MW Power Oy
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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
    • F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
    • F28D7/02—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being helically coiled
    • F28D7/024—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being helically coiled the conduits of only one medium being helically coiled tubes, the coils having a cylindrical configuration
    • 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
    • F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
    • F28D7/04—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being spirally coiled
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K25/00—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for
    • F01K25/08—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for using special vapours
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F22—STEAM GENERATION
    • F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
    • F22B1/00—Methods of steam generation characterised by form of heating method
    • F22B1/02—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers
    • F22B1/18—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers the heat carrier being a hot gas, e.g. waste gas such as exhaust gas of internal-combustion engines
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F22—STEAM GENERATION
    • F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
    • F22B37/00—Component parts or details of steam boilers
    • F22B37/02—Component parts or details of steam boilers applicable to more than one kind or type of steam boiler
    • F22B37/10—Water tubes; Accessories therefor
    • F22B37/14—Supply mains, e.g. rising mains, down-comers, in connection with water tubes
    • F22B37/142—Supply mains, e.g. rising mains, down-comers, in connection with water tubes involving horizontally-or helically-disposed water tubes, e.g. walls built-up from horizontal or helical tubes

Definitions

  • the invention refers to a heat exchanger unit according to the preamble of claim 1 for recovering heat from a hot gas flow to a medium flow
  • heat exchanger unit comprises an enclosure structure, a gas flow inlet, in which the gas is adapted to flow in a substantially vertical direction, and a gas flow outlet, in which heat exchanger unit the enclosure structure encompasses several pipe spiral heat exchangers provided with an essentially gas-tight wall and arranged at least partially within each other with respect to the longitudinal axis of the enclosure structure so that the gas flow is arranged to pass respectively in an annular space, which is formed of two within each other arranged heat exchangers.
  • Such a heat exchanger unit is known from US 3351041 A1 .
  • Especially the invention relates to an evaporator for an organic medium.
  • ORC Organic Rankine Cycle
  • ORC Organic Rankine Cycle
  • a suitable organic medium for instance toluene, isobutane or isopenthane, is used as a circulation medium instead of water.
  • the ORC process is particularly applicable on a relatively low temperature level, whereby waste heat released even at a low temperature may be utilised.
  • an intermediate hot oil circuit is often used between hot flue gases and a vaporisable medium.
  • heat is transferred from the flue gas to the hot oil in a separate thermal oil vessel, from which the heated liquid hot oil is pumped to an evaporator for an organic circulation medium, in which the heat is transferred further from the liquid hot oil to the organic circulation medium.
  • the publication FI 86464 discloses, on a principle level, an ORC power station, in which the evaporator for an organic medium is in direct heat transfer connection with hot gas.
  • the problem involved in the evaporation of the organic medium directly by hot gas, especially by the boiler's flue gases or the like, which reacts slowly to power adjustment, is how to avoid both the excessive heating of the evaporator material and the overheating of the organic medium, which would lead to chemical changes in the substance, such as cracking of hydrocarbons, especially in transient situations. In such a case the overheating of the organic medium, in particular, would bring about detrimental changes in its flowing and heat transfer properties.
  • a purpose of the invention is to provide a heat exchanger unit, which is suitable for evaporating and/or heating an organic medium by hot gas, especially by flue gas from combustion of biomass.
  • the heat exchanger unit according to the invention for recovering heat from a hot gas flow to a medium flow comprises an enclosure structure, a gas flow inlet, in which the gas is adapted to flow in a substantially vertical direction, and a gas flow outlet, in which heat exchanger unit the enclosure structure encompasses several heat exchangers provided with an essentially gas-tight wall and arranged at least partially within each other with respect to the longitudinal axis of the enclosure structure so that the gas flow is arranged to pass respectively in a space, which is formed of two within each other arranged heat exchangers.
  • the invention is characterised by the enclosure structure comprising a bottom section, against which the heat exchangers are mainly supported by means of a support arrangement, and the support arrangement comprising an opening surface in at least one of the heat exchangers for allowing the through-flow of the gas from first side of the heat exchanger to a second side thereof.
  • the support arrangement of the heat exchangers is made of a cooled structure, in which the medium flow of the heat exchanger is adapted to flow.
  • the heat exchangers are pipe spiral heat exchangers and the cooled structure of the support arrangement comprises an take-off shaped as a flow elbow formed of a pipe spiral.
  • an opening surface is formed and arranged to extend to a distance from the inner surface of the bottom section of the enclosure structure, whereby an ash space is formed in the area above the bottom section extending from the inner surface of the bottom section to the lower edge of the opening surface.
  • the size of the ash space is so large that it also acts as a service space, through which required reparations can be performed as well. Then, the size of the space is such that a serviceman has enough room to work therein. There must be several openings, typically e.g. four, to form the opening surface as well as corresponding outer service doors/ash pit doors.
  • the opening surface in each heat exchanger is defined so that the total of the cross-sectional surfaces of individual (radial) openings is larger than the cross-sectional flow area of the heat exchanger's annular space (space between the heat exchangers arranged within each other), whereby the pressure loss of the gas flow in the openings is smaller than or equal with the pressure loss in the annular space between the heat exchangers within each other.
  • the ratio between the height and the radial width of the ash space is larger than 1 and the ash settled in the ash space during operation will normally not be re-entrained with the gas.
  • the heat exchanger unit comprises preferably several ash removal conduits that can be opened to the ash space.
  • An ash removal conduit comprises a substantially gas-tight channel penetrating gas-tightly the support arrangement of the heat exchanger, whereby it does not in normal use disturb the flowing of the gas in the heat exchanger unit.
  • the heat exchanger unit is arranged to heat and/or evaporate an organic medium, whereby the last one of the heat exchangers arranged within each other is adapted to be the first heat exchanger in the medium flow and the first one of the heat exchangers arranged within each other is adapted to be the second heat exchanger in the medium flow.
  • a heat exchanger unit 1 produces superheated vapour for a turbine 5, which drives a high speed generator 4, which is connected to an electric network 2 by means of a frequency converter 3.
  • a frequency converter 3 for the organic mediums applicable at the moment toluene is particularly suitable to be used as an organic medium in conjunction with the present invention. Since a biomass fuel boiler is an important target of application of the invention, hot gas or a gas flow can also be referred to as flue gas in the following.
  • From the turbine 5 the toluene vapour is led to a recuperator 6, in which a liquid toluene to be introduced to the heat exchanger unit 1 is pre-heated by the toluene vapour.
  • the task of the recuperator 6 is to eliminate the superheat in the vapour coming from the turbine, as toluene vapour is characterised by still being superheated after the expansion in the turbine.
  • the toluene vapour is introduced into a condenser 7, in which it is condensed to form a liquid, and in which also the rest of the superheat is eliminated in case the vapour is still superheated after the recuperator.
  • the liquid toluene is introduced into a condensation tank 8, from which it is led further at raised pressure via a pre-feed pump 9 and a feed pump 10 to the recuperator 6.
  • the toluene vapour heats the liquid toluene and thereafter it is fed to the heat exchanger unit 1, in which the toluene is further heated, evaporated and the vapour is superheated.
  • the heat exchanger unit 1 is arranged directly into a hot gas flow 11, which in this application is flue gas from combustion of biomass, and the heat exchanger unit is therefore connected with a biomass boiler 13.
  • Fig. 1 also shows the heat exchanger unit 1 according to the invention, in which heat is transferred to the first heat exchanger in the flow direction of the organic medium thus cooling the gas flow to its final temperature.
  • FIG. 2 shows one embodiment of the heat exchanger unit 1 according to the invention.
  • Fig. 2 shows the cross-section of the heat exchanger unit in such a manner that the left side, in the figure, of a longitudinal axis 26 represents mainly the support of the heat exchangers and the flow arrangement on the gas side and the right side, in the figure, shows the interconnection of the heat exchangers.
  • the heat exchanger unit comprises heat exchangers 21, 22, 23 24 arranged within each other and formed of pipe spirals 20.
  • the heat exchangers are preferably symmetrical with respect to the cross-section of the longitudinal axis, and as pipe spirals mainly cylindrical.
  • the type of the heat exchanger unit is according to the invention a once-through evaporator.
  • the organic medium is arranged to flow in the piping of the heat exchangers and the gas outside the pipes of the heat exchangers.
  • Fig. 2 shows a heat exchanger unit, which is formed within an enclosure structure consisting of an outer shell 30, a cover section 31' and a bottom section 31.
  • the heat exchanger unit comprises a gas flow inlet 25', which is parallel with the heat exchanger unit's longitudinal axis 26 and located in the middle of the heat exchanger unit.
  • the innermost heat exchanger 22 with respect to the longitudinal axis 26 of the heat exchanger unit forms an after-burning space 25, which is located above the actual furnace of the boiler 13 ( Fig. 1 ).
  • the after-burning space 25 the after-burning of the flue gas and the solid matter particles therein coming form the furnace takes place, and therefore there are feed members 12 arranged in the after-burning space 25 for bringing air (or oxygenous gas) into the hot gas.
  • air or oxygenous gas
  • the flue gases are led into annular channels formed between the heat exchangers 21 - 24 arranged within each other parallel with the longitudinal axis.
  • the heat is transferred to the heat exchanger 22 mainly as thermal radiation, whereas thereafter, in the less hot sections in the gas flow direction, convective heat exchange is dominant.
  • every second heat exchanger 21, 23 comprises an opening surface 28 in its lower part, which opening surface enables the gas to flow from first side of said heat exchanger to the second side thereof, i.e. to move radially closer to the outer section.
  • the gas flow in said opening surface is sufficiently weak to prevent the ash on the bottom of the ash spaces from being entrained to any substantial extent back to the gas flow.
  • the support consists of cooled support structures formed of pipes and flow elbows so that the flue gas may pass between them from the channel formed of pipe spirals 20 to the next channel in the direction of the radius of the heat exchanger unit.
  • the organic medium flowing in the pipes and flow elbows forming the structure is used for cooling the support structure. In practise, this can be accomplished and the opening surface formed so that the heat exchanger is supported against the bottom section 31 of the enclosure structure of the heat exchanger unit by means of a heat exchange pipe or pipes by arranging an take-off as a u-shaped flow elbow in the pipe located in the lower section. This is shown also in Figs. 5 and 6 .
  • these structures also make it possible to form routes required by the cleaning of the heat exchange surfaces and gas flues between the pipe spirals 20 as well as the ash spaces 39 below them.
  • a heat exchanger which instead comprises an opening surface 28' at the end of the cover part 31' of the enclosure structure, i.e. above itself.
  • This kind of a heat exchanger is made substantially gas-tight in its lower part, for instance by means of a refractory lining or brick-laying, which is though, preferably, a cooled structure.
  • the flue gases are discharged from the heat exchanger unit via a gas outlet 36, which in the embodiment of Fig. 1 is located on the outer rim of the unit.
  • the heat exchanger unit is an intermediate form of a counter flow heat exchanger and a parallel flow heat exchanger, since the directions of the flue gas flows outside (two annular spaces) the medium (in a spiral pipe) to be heated are opposite.
  • the organic medium is first led via a conduit 35 to the first heat exchanger 21, in which the organic medium is heated by hot flue gas thus cooling the gas flow to its final temperature.
  • the liquid organic medium coming to the heat exchanger unit is led to the less hot part on the flue gas side.
  • the organic medium flows mainly counter-currently with respect to the gas so as to make the heat exchange surface as small as possible.
  • the second heat exchanger is the innermost of the heat exchangers arranged within each other.
  • the second heat exchanger 22 is further connected to the third heat exchanger 23 via a connecting pipe 22'.
  • the third heat exchanger 23 acts primarily as an evaporator.
  • It is further connected to the fourth heat exchanger 24 via a connecting pipe 23', in which exchanger the superheating of the vapour takes place.
  • all the rest of the heat exchangers are arranged radially in the space between the first and the second heat exchanger, symmetrically with respect to the longitudinal axis 26.
  • the superheated vapour is discharged from the section on the flue gas side, in which the flue gas is not at its hottest.
  • the vapour is primarily superheated by the fourth heat exchanger 24, which is located between the innermost 22 and the outermost 21 of the heat exchangers arranged within each other.
  • the fourth heat exchanger 24 is provided with an outlet 37 for the organic medium in the upper part of the pipe spiral 20.
  • the lower parts of the outer shell 30 of the heat exchanger unit and the structures 28, 33 guiding the flue gas flow are provided with ash removal doors 38, which are used for cleaning the flue gas side of the heat exchanger unit.
  • the lower parts of the pipe spirals 20 form in the vertical direction a radially staggered structure so that also the cleaning of the channels formed by the inner pipe spirals is possible via the ash removal doors 38, which act as ash removal conduits. This is shown in more detail in Figs. 3 and 4 .
  • the ash removal door is provided with a substantially gas-tight channel 38', which extends to the innermost ash space 39.
  • FIG. 4 shows an embodiment, in which a door 38", which can be opened and closed, is arranged in conjunction with the structures guiding the flue gas flow of the heat exchanger 24 for cleaning the ash space.
  • the ash removal doors are located so as to make it possible to perform the cleaning efficiently.
  • the cleaning in operation is performed automatically by dropping the fouling collected on the heat exchange surfaces and other parts of the gas flues on the flue gas side, to the lower parts of the flue gas side by using a cleaning method appropriate for the situation.
  • the ash spaces 39 are formed of the structures in the lower parts of the flue gas side, into which spaces collected fouling can be discharged in the cleaning during a shutdown via the above-mentioned ash removal doors 38.
  • the ash space is formed in the lower part of the structures 28, 33 guiding the flue gas flow so that the opening surface 28 in the vicinity of the bottom section 31 of the heat exchanger unit extends from the bottom section at least so that the total cross-sectional flow surface of the openings corresponds to the cross-sectional flow area between the pipe spirals.
  • Figs. 5 and 6 show an advantageous pipe structure, in which the supporting of the heat exchangers 21 - 24 and the cooling of the structures 28, 33 guiding the flue gas flow is provided according to the invention.
  • a u-shaped part 32 arranged to extend downwards from the lower surface of the spiral, which u-shaped part acts as a cooling and supporting structure for the heat exchangers.
  • Fig. 7 illustrates the heating and/or evaporating an organic medium, by way of example, by toluene.
  • the vertical axis represents the temperature T and the horizontal axis the relative heat flow q of the gas.
  • Graph 72 illustrates the temperature of the toluene and its development, when it passes through several successive heat exchangers.
  • the numerical values given for the temperatures in the following are values in one specific case, which are presented here only for facilitating the understanding of the invention.
  • the organic medium, toluene in this case, is brought to the first heat exchanger 21 at a temperature of 156 °C, which in this example corresponds to the final temperature of 350 °C of the exiting gas.
  • Toluene is heated in the first heat exchanger 21 to a temperature of 196 °C, while the temperature of the incoming gas is 475 °C. This is performed mainly by heat transfer of counter-flow type, whereby the surface area of the heat exchanger required for the heating is minimised.
  • the toluene is heated further in the second heat exchanger 22 to a temperature of 300 °C, but now the heat source is the gas, which starts the cooling of the gas flow from its initial temperature, in this case 1100 °C, and cools the gas down to a temperature of 755 °C.
  • the heat source is the gas, which starts the cooling of the gas flow from its initial temperature, in this case 1100 °C, and cools the gas down to a temperature of 755 °C.
  • the heat exchanger is primarily a parallel flow heat exchanger.
  • the toluene is introduced into the evaporator section, which consists mainly of the third heat exchanger 23.
  • the evaporation lowers the gas temperature to 570 °C.
  • the vapour is superheated, in this example to a temperature of 326 °C, whereby the temperature of the flue gas is 475 °C, i.e. it is in the state, in which the heat transfer by the first heat exchanger starts.
  • the pipe spiral may, deviating from the embodiments shown in the figures, be made of a pair of pipes or of several adjacent pipes instead of one pipe.

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Sustainable Development (AREA)
  • Sustainable Energy (AREA)
  • Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)

Claims (6)

  1. Échangeur thermique pour transférer la chaleur d'un flux de gaz chaud vers un écoulement de fluide, lequel échangeur thermique comprend un boîtier (30, 31,31'), une entrée du flux de gaz (25'), où le gaz est adapté pour s'écouler dans une direction sensiblement verticale, et une sortie du flux de gaz (36), où le boîtier de l'échangeur thermique contient plusieurs échangeurs thermiques en spirale de tuyaux (21, 22, 23, 24) pourvus d'une paroi étanche aux gaz et agencés au moins partiellement les uns à l'intérieur de l'autre par rapport à l'axe longitudinal (26) du boîtier, de telle sorte que le flux de gaz passe à chaque fois dans un espace formé de deux échangeurs thermiques disposés l'un dans l'autre, caractérisé en ce que le plus externe des échangeurs thermiques de chaleur disposés l'un dans l'autre est agencé pour être le premier échangeur thermique (21) dans la direction d'écoulement du fluide et le plus interne des échangeurs thermiques disposés l'un dans l'autre est agencé pour être le deuxième échangeur thermique (22) dans la direction d'écoulement du fluide, en ce que le fluide est évacué de l'échangeur thermique à partir d'un échangeur thermique situé entre le plus interne et le plus externe des échangeurs thermiques, en ce que le boîtier contient une section inférieure (31') qui porte principalement les échangeurs thermiques par l'intermédiaire d'un dispositif de support (32) constitué d'une structure de refroidissement (32), qui a une forme de décollage comme un coude d'écoulement formé d'un tuyau en spirale et dans laquelle le débit moyen de l'échangeur thermique est adapté à l'écoulement, et en ce que le dispositif de support comprend une surface d'ouverture (28) dans au moins l'un des échangeurs thermique pour permettre l'écoulement du gaz à partir de la première extrémité de l'échangeur thermique à la seconde extrémité de celui-ci.
  2. Échangeur thermique selon la revendication 1, caractérisé en ce que la surface d'ouverture (28) est agencée pour s'étendre à une certaine distance de la surface interne de la section inférieure du boîtier ; ainsi, un espace de cendres (39) est formée dans la zone au-dessus de la section inférieure s'étendant à partir de la surface interne de la section inférieure à l'extrémité inférieure de la surface d'ouverture.
  3. Échangeur thermique selon la revendication 2, caractérisé en ce que la somme des surfaces de section transversale des ouvertures individuelles formant la surface d'ouverture est plus grande que la surfaces de section transversale totale de l'espace annulaire.
  4. Échangeur thermique selon la revendication 2, caractérisé en ce que l'échangeur thermique comprend plusieurs conduits d'évacuation des cendres (38) qui peuvent donner sur l'espace de cendres (39).
  5. Échangeur thermique selon la revendication 4, caractérisé en ce qu'un conduit d'évacuation des cendres (38) comprend un canal sensiblement étanche aux gaz pénétrant de façon étanche aux gaz dans le dispositif de support de l'échangeur thermique.
  6. Échangeur thermique selon l'une quelconque des revendications 1 à 5, caractérisé en ce qu'il est adapté pour chauffer et / ou faire s'évaporer un fluide organique.
EP06808029.0A 2005-12-30 2006-11-10 Unite d'echangeur de chaleur destinee a recuperer de la chaleur a partir d'un ecoulement de gaz chaud Not-in-force EP1966559B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FI20055718A FI120557B (fi) 2005-12-30 2005-12-30 Lämmönsiirrinyksikkö lämmön talteenottamiseksi kuumasta kaasuvirtauksesta
PCT/FI2006/050488 WO2007077293A1 (fr) 2005-12-30 2006-11-10 Procede de chauffage et / ou d'evaporation d'un milieu organique et unite d'echangeur de chaleur destinee a recuperer de la chaleur a partir d'un ecoulement de gaz chaud

Publications (3)

Publication Number Publication Date
EP1966559A1 EP1966559A1 (fr) 2008-09-10
EP1966559A4 EP1966559A4 (fr) 2011-10-19
EP1966559B1 true EP1966559B1 (fr) 2013-05-22

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EP06808029.0A Not-in-force EP1966559B1 (fr) 2005-12-30 2006-11-10 Unite d'echangeur de chaleur destinee a recuperer de la chaleur a partir d'un ecoulement de gaz chaud

Country Status (6)

Country Link
EP (1) EP1966559B1 (fr)
CA (1) CA2632275C (fr)
FI (1) FI120557B (fr)
RU (1) RU2403522C2 (fr)
UA (1) UA92777C2 (fr)
WO (1) WO2007077293A1 (fr)

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US8181463B2 (en) * 2005-10-31 2012-05-22 Ormat Technologies Inc. Direct heating organic Rankine cycle
EP2202474B1 (fr) 2008-12-23 2011-06-29 Kronotec AG Installation de séchage de produit de concassage du bois
IT1397145B1 (it) * 2009-11-30 2013-01-04 Nuovo Pignone Spa Sistema evaporatore diretto e metodo per sistemi a ciclo rankine organico.
WO2012129079A1 (fr) * 2011-03-21 2012-09-27 The Penn State Research Foundation Brûleur à haut rendement et interface de moteur thermique à cycle fermé
CN102147105B (zh) 2011-04-11 2012-11-21 中国华能集团清洁能源技术研究院有限公司 适用于超高汽温蒸汽参数的倒置煤粉锅炉布置结构
RU2609273C2 (ru) * 2015-06-17 2017-02-01 Общество С Ограниченной Ответственностью "Промвектор" Электрогенерирующий комплекс "СКАТ"
CN108534569B (zh) * 2018-04-20 2024-03-29 杨艺 一种高效热交换器
CN110513669B (zh) * 2019-08-23 2021-02-26 七台河宝泰隆新能源有限公司 一种蒸汽发生器重油温度调节装置

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CA2632275C (fr) 2013-10-01
FI20055718A0 (fi) 2005-12-30
RU2008131292A (ru) 2010-02-10
FI20055718L (sv) 2007-07-01
UA92777C2 (ru) 2010-12-10
FI120557B (fi) 2009-11-30
RU2403522C2 (ru) 2010-11-10
WO2007077293A1 (fr) 2007-07-12
CA2632275A1 (fr) 2007-07-12
EP1966559A4 (fr) 2011-10-19
EP1966559A1 (fr) 2008-09-10

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