EP2449264B1 - Dispositif de transport de fluides par des pompes centrifuges - Google Patents

Dispositif de transport de fluides par des pompes centrifuges Download PDF

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Publication number
EP2449264B1
EP2449264B1 EP10726092.9A EP10726092A EP2449264B1 EP 2449264 B1 EP2449264 B1 EP 2449264B1 EP 10726092 A EP10726092 A EP 10726092A EP 2449264 B1 EP2449264 B1 EP 2449264B1
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Prior art keywords
fluid
centrifugal pump
entry
pressure
state
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German (de)
English (en)
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EP2449264A1 (fr
Inventor
Gerhard Schwarz
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KSB SE and Co KGaA
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KSB AG
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F04—POSITIVE - DISPLACEMENT MACHINES FOR LIQUIDS; PUMPS FOR LIQUIDS OR ELASTIC FLUIDS
    • F04D—NON-POSITIVE-DISPLACEMENT PUMPS
    • F04D7/00—Pumps adapted for handling specific fluids, e.g. by selection of specific materials for pumps or pump parts
    • F04D7/02—Pumps adapted for handling specific fluids, e.g. by selection of specific materials for pumps or pump parts of centrifugal type
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F04—POSITIVE - DISPLACEMENT MACHINES FOR LIQUIDS; PUMPS FOR LIQUIDS OR ELASTIC FLUIDS
    • F04D—NON-POSITIVE-DISPLACEMENT PUMPS
    • F04D13/00—Pumping installations or systems
    • F04D13/12—Combinations of two or more pumps
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F04—POSITIVE - DISPLACEMENT MACHINES FOR LIQUIDS; PUMPS FOR LIQUIDS OR ELASTIC FLUIDS
    • F04D—NON-POSITIVE-DISPLACEMENT PUMPS
    • F04D25/00—Pumping installations or systems
    • F04D25/16—Combinations of two or more pumps ; Producing two or more separate gas flows
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F04—POSITIVE - DISPLACEMENT MACHINES FOR LIQUIDS; PUMPS FOR LIQUIDS OR ELASTIC FLUIDS
    • F04D—NON-POSITIVE-DISPLACEMENT PUMPS
    • F04D29/00—Details, component parts, or accessories
    • F04D29/58—Cooling; Heating; Diminishing heat transfer
    • F04D29/586—Cooling; Heating; Diminishing heat transfer specially adapted for liquid pumps
    • 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
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10T—TECHNICAL SUBJECTS COVERED BY FORMER US CLASSIFICATION
    • Y10T137/00—Fluid handling
    • Y10T137/0318—Processes
    • Y10T137/0396—Involving pressure control

Definitions

  • the invention relates to a method for conveying fluids with centrifugal pumps, wherein before a centrifugal pump, machines and / or apparatus are arranged, which influence the pressure and / or the temperature of the fluid. Furthermore, the invention relates to a process for the sequestration of carbon dioxide, wherein the carbon dioxide is brought to a suitable for a proposed reservoir pressure and / or temperature and is conveyed into the deposit.
  • the burning of fossil fuels in power plants generates carbon dioxide, which is responsible for the greenhouse effect.
  • the aim is therefore to reduce the emission of carbon dioxide into the atmosphere.
  • An effective measure is the sequestration of carbon dioxide.
  • the carbon dioxide produced in the power plants is separated and sent to landfill.
  • Deposits are geological formations such as oil reservoirs, natural gas deposits, saline aquifers or coal seams. Also a storage in the deep sea is examined.
  • the pump system comprises a multi-stage pump, like an underwater motor pump, which is arranged in a pot housing. This arrangement relies on a closed conveyor system in which very high pump inlet pressures prevail. Due to the above-mentioned boundary conditions, the carbon dioxide to be produced is exclusively in the liquid phase.
  • the system is being used for Enhanced Oil Recovery (EOR), injecting carbon dioxide into oil fields to increase the yield of extracted oil.
  • EOR Enhanced Oil Recovery
  • the system also serves to sequester carbon dioxide.
  • the WO 99/41490 A1 and the WO 2005/052365 A2 also describe systems for promoting supercritical carbon dioxide.
  • the US 2005/0155378 A1 describes a system for producing high purity carbon dioxide.
  • the object of the present invention is to provide a method which allows the promotion of supercritical fluids with centrifugal pumps, with the certainty of avoiding impermissible density changes of the fluid to be delivered.
  • This object is achieved in that by means of the machines and / or apparatus of the entry state of the fluid is adjusted in the centrifugal pump so that the fluid in the centrifugal pump only assumes conditions in which the real gas factor of the fluid has already reached or exceeded its minimum.
  • the real gas factor While for real gases the real gas factor is one, it deviates for real gases depending on pressure and temperature.
  • the real gas factor below the so-called Boyle temperature, initially decreases with increasing pressure, reaches a minimum and then increases again.
  • the inventive method ensures that the fluid assumes only conditions in the centrifugal pump, in which the real gas factor has already reached or exceeded its minimum. Operating the centrifugal pump in this allow operating areas, so a discontinuous pumping behavior and damage to the centrifugal pump, in the promotion of supercritical fluids are excluded with certainty.
  • a boundary line for the operation of centrifugal pumps is defined for the first time for the supercritical region, which must not be undershot during production.
  • centrifugal pump During the pumping process, there are pressure increases and temperature increases in the centrifugal pump.
  • the conditions which a fluid assumes in the centrifugal pump depend on the delivery situation and the type of centrifugal pump used. These are usually known to the operator.
  • the machines and apparatus used in the method configure the entry state of the fluid so that its real gas factor has already reached or exceeded its minimum at least at the entrance to the centrifugal pump.
  • the fluid may be present in the process already at the entrance to the centrifugal pump in a supercritical state. Likewise, it is possible for the fluid to be initially liquid when entering the centrifugal pump and to assume a supercritical state only in the centrifugal pump. Also in this case, the boundary line according to the invention is observed.
  • the inlet state of the fluid is set with compressors and heat exchangers. It proves to be advantageous if the fluid passes through at least one compression and one cooling stage. The number of compression and cooling stages sets the entry state of the fluid into the centrifugal pump.
  • the state of entry of the fluid at the inlet into the suction port of the centrifugal pump is generally considered to be the entry state. However, at the latest when the fluid enters the impeller, an entry state according to the invention must be reached.
  • the inlet temperature and / or the inlet pressure of the fluid are measured and forwarded to a control and / or regulating unit.
  • a control and / or regulating unit commercially available controllers or controllers can be used. It is also conceivable to use a process control system.
  • the control and / or regulating unit can be used to specifically influence the machines and apparatus in order to determine the state of entry of the Adjust fluids.
  • the control and / or regulating unit sends signals to the machines and apparatuses. The signals influence the drive motors or the actuators of the machines and apparatuses.
  • control and / or regulating unit triggers an alarm when the real gas factor of the fluid at the inlet to the pump has not yet reached its minimum.
  • the system can be brought into a safety position. This can also lead to a shutdown of the centrifugal pump.
  • Fig. 1 a flow chart of the method according to the invention is shown as a schematic representation.
  • the fluid here carbon dioxide, initially enters a compressor 1.
  • the compressor 1 is driven by a motor 2.
  • This schematic diagram applies to single or multi-stage compressor designs.
  • the number of compressor and heat exchanger stages varies. For reasons of clarity, only 2 process stages are shown here; but usually there are several.
  • the fluid In the compressor 1, the fluid is brought to a higher pressure, wherein the temperature of the fluid increases. After the compressor 1, the fluid enters a heat exchanger 3. The flowed through by coolant heat exchanger 3, absorbs heat from the fluid flow and thus lowers its temperature. The amount of coolant is adjusted with a valve 4. As an actuator, the valve 4 is operated with a motor 5.
  • the carbon dioxide can enter another compressor 6 or in another compressor stage, which is operated here with a motor 7.
  • the fluid undergoes a renewed increase in pressure and temperature before it enters a further heat exchanger 8, which may also be designed as an intercooler.
  • the carbon dioxide stream is cooled again. This is also done with a coolant flow, which is regulated via a valve 9, which has a motor 10 as an actuator.
  • the inlet state of the fluid into the centrifugal pump 11 is set via the machines 1, 6 and apparatuses 3, 8 so that the fluid in the centrifugal pump 11 assumes only conditions in which the real gas factor has already reached or exceeded its minimum.
  • the aggregate states of the fluid are detected at the entrance to the centrifugal pump 11 by means of conventional pressure and temperature measuring points 13, 14.
  • the measuring points 13, 14 are connected to a control unit 15, which controls the machines 1, 6 and apparatuses 3, 8.
  • the control unit 15 ensures that before the centrifugal pump 11 those aggregate states are set, due to which the centrifugal pump can be operated without damage.
  • the motor 12 of the centrifugal pump 11 can be influenced by the control unit 15, if it is designed accordingly.
  • Advantageous for the process is the use of variable speed motors. This depends on the given boundary conditions of the process or its installation.
  • the pressure measuring point 13 indicated by the abbreviation PI, measures the pressure of the carbon dioxide. If there is the danger that the carbon dioxide within the centrifugal pump 11 assumes states in the forbidden range at which the real gas factor has not yet reached its minimum, then its signals are forwarded via the control point 15 to the motors 2, 7 of the compressors 1, 6, via which the pressure of the carbon dioxide is adjustable.
  • the carbon dioxide leaves the centrifugal pump 11 in a state required for the subsequent process.
  • high pressure differences in the centrifugal pump can be realized without additional intermediate cooling with the inventive method.
  • a diagram is shown in which for a fluid to be conveyed carbon dioxide whose real gas factor z is plotted as a function of the pressure p.
  • the state of entry of the fluid by means of the machines 1, 6 and / or apparatuses 3, 8 is set so that the fluid when flowing through the centrifugal pump 11 assumes only states in which the real gas factor has already reached or exceeded its minimum.
  • the real gas factor of the fluid remains the same or increases.
  • an operating curve 16 is shown for a centrifugal pump 11, in which both the entry state E, and the exit state A of the fluid are within the permitted range.
  • the fluid is present at the entrance to the centrifugal pump 11 in a state in which the real gas factor z has already exceeded its minimum.
  • the pressure p and the temperature T of the fluid change.
  • the fluid enters the pump 11 at a pressure of 95 bar and leaves the pump 11 at a pressure of 300 bar.
  • the inlet temperature of the fluid is about 35 ° C and the outlet temperature of the fluid is about 70 ° C.
  • the entry state of the fluid through the machines 1, 6 and / or the apparatuses 3, 8 has been adjusted so that the fluid in the centrifugal pump 11 only assumes conditions in which the real gas factor z has already reached or exceeded its minimum.
  • a bold solid boundary curve 17 is defined for pumpable fluids in the supercritical region.
  • This supercritical region is to the right of the supercritical point kP of the fluid.
  • the limit curve 17 for the operation of centrifugal pumps is thereby defined for the supercritical region.
  • the carbon dioxide may take in the centrifugal pump 11 only states that are on this limit curve 17 or to the right. In this area, the real gas factor of carbon dioxide has already reached or exceeded its minimum.
  • the operating curve 16 of the centrifugal pump 11 is completely within the permitted range.
  • Fig. 3 shows a diagram in which the product p ⁇ v is plotted as a function of the pressure p for carbon dioxide.
  • the product p ⁇ v can be considered analogous to the real gas factor z. While the isotherms run horizontally for ideal gas behavior, real gases show a behavior that occurs in Fig. 3 is shown with dashed isotherms.
  • the product p ⁇ v on an isotherm with increasing Pressure smaller until a minimum is reached. After passing through the respective minimum, the product p ⁇ v increases again with increasing pressure.
  • the product p ⁇ v increases approximately linearly.
  • the entry state of the fluid with the aid of machines 1, 6 and / or apparatuses 3, 8 is adjusted so that the product p ⁇ v of the fluid in the centrifugal pump 11 has already reached or exceeded its minimum.
  • FIG. 3 an operating curve 16 is shown for a centrifugal pump 11, in which both the entry state E, and the exit state A of the fluid are within the permitted range.
  • the fluid has at the entrance to the pump 11 a state in which the real gas factor z has already exceeded its minimum.
  • the pressure p and the temperature T of the fluid change.
  • the fluid enters the pump at a pressure of 95 bar and leaves the pump at a pressure of 300 bar.
  • the inlet temperature of the fluid is about 35 ° C.
  • the outlet temperature of the fluid is 70 ° C.
  • the entry state of the fluid through machines 1, 6 and / or apparatuses 3, 8 has been set so that the fluid in the centrifugal pump 11 assumes only conditions in which the real gas factor z of the fluid has already reached or exceeded its minimum.
  • the operating curve 16 is completely within the permitted range. Analogous to Fig. 2 Here, too, the surge limit is shown as a bold solid limit curve 17.
  • FIGS. 4a . 4b and 4c show the phase diagram of carbon dioxide, which is often referred to as a state diagram or pT diagram.
  • the supercritical state ük is also shown. It can be seen from the diagram that carbon dioxide can not be liquid at a standard pressure of 1.013 bar, but only a sublimation at -78.5 ° C is observed. Carbon dioxide can be liquid only at higher pressures.
  • the vapor pressure curve 18 represents a limit line for the operating states that the fluid may take in the centrifugal pump.
  • the liquid carbon dioxide must not assume any conditions in the centrifugal pump at which the vapor pressure curve 18 is reached or exceeded, since otherwise cavitation occurs in the centrifugal pump.
  • the vapor pressure curve 18 is limited by the triple point TP and the critical point kP.
  • Fig. 4a When displayed in Fig. 4a is the entry state E of the fluid to be delivered in the permitted range.
  • the fluid has at the entrance to the centrifugal pump 11 a state in which the real gas factor z has already exceeded its minimum.
  • the pressure and the temperature of the fluid change.
  • the fluid enters the pump at a pressure of 95 bar and leaves the pump at a pressure of 220 bar.
  • the inlet temperature of the fluid is 35 ° C.
  • the outlet temperature of the fluid is 59 ° C.
  • the state of entry of the fluid through machines 1, 6 and / or apparatuses 3, 8 has been adjusted so that the fluid in the centrifugal pump 11 assumes only conditions in which the real gas factor of the fluid has already reached or exceeded its minimum.
  • the operating curve 16 lies completely within the allowed supercritical range divided by the limit curve 17. In this presentation of the Fig. 4a is located to the left of the limit curve 17 of the allowable pump range.
  • the entry state was varied by the machines 1, 6 and / or apparatuses 3, 8 so that the fluid enters the centrifugal pump 11 at a lower inlet temperature T.
  • the entire operating curve shifts from 16 to 16, so that now according to the invention the fluid in the centrifugal pump 11 assumes only states in which the real gas factor z has already reached or exceeded its minimum.
  • a higher inlet pressure p can be set. All states are in the allowed range after this variation of the entry state.
  • the exit state A is in the forbidden range.
  • the fluid is initially present at the inlet to the pump in a state in which the real gas factor z has already exceeded its minimum.
  • the pressure and the temperature of the fluid change.
  • the fluid enters the pump at a pressure of 95 bar and leaves the pump at a pressure of 220 bar.
  • the inlet temperature of the fluid is 35 ° C.
  • the outlet temperature of the fluid is 130 ° C.
  • the operating states of the fluid take from the intersection V of the operating curve 16 with the bold and solid drawn limit curve 17 values at which the real gas factor of the fluid has not yet reached or exceeded its minimum.
  • the operating curve is in the forbidden range.
  • the inlet state of the fluid by means of the machines 1, 6 and apparatuses 3, 8 is varied so that the entire operating curve 16 is within the permitted range, ie that the fluid in the centrifugal pump only assumes conditions in which the real gas factor of the fluid already be Minimum has reached or exceeded.
  • the entry point E of the curve 16 is shifted further to the right, so that the fluid enters the centrifugal pump 11 at a lower inlet temperature at the entry point E '.
  • the entire, here inadmissible operating curve 16 shifts as a new and permissible operating curve 16 'in the allowed supercritical range.
  • a higher inlet pressure p can be set.
  • the fluid in the centrifugal pump now only assumes conditions in which the real gas factor has already reached or exceeded its minimum. All states are in the allowed range after this variation of the entry state.

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Structures Of Non-Positive Displacement Pumps (AREA)
  • Feeding, Discharge, Calcimining, Fusing, And Gas-Generation Devices (AREA)
  • Control Of Positive-Displacement Pumps (AREA)
  • Control Of Non-Positive-Displacement Pumps (AREA)
  • Reciprocating Pumps (AREA)

Claims (15)

  1. Procédé de transport de fluides par des pompes centrifuges (11), dans lequel des machines (1, 6) et/ou des appareils (3, 8) sont disposés avant une pompe centrifuge (11), lesquels influencent la pression et/ou la température du fluide, caractérisé en ce que l'on mesure la température d'entrée (T) et/ou la pression d'entrée (p) du fluide et on la retransmet à une unité de commande et/ou de régulation (13, 14), dans lequel l'unité de commande et/ou de régulation (13, 14) retransmet aux machines (1, 6) et/ou aux appareils (3, 8) des signaux par lesquels l'état d'entrée du fluide peut être réglé, dans lequel on règle au moyen des machines (1, 6) et/ou des appareils (3, 8) l'état d'entrée du fluide dans la pompe centrifuge (11), de telle manière que le fluide ne prenne dans la pompe centrifuge (11) que des états dans lesquels le facteur de compressibilité (z) du fluide a déjà atteint ou dépassé son minimum.
  2. Procédé selon la revendication 1, caractérisé en ce que le fluide se trouve à l'entrée dans la pompe centrifuge (11) et/ou dans la pompe centrifuge (11) dans un état hypercritique.
  3. Procédé selon la revendication 1 ou 2, caractérisé en ce que, lors d'une augmentation de la pression dans la pompe centrifuge (11), le facteur de compressibilité (z) du fluide reste constant ou augmente.
  4. Procédé selon l'une quelconque des revendications 1 à 3, caractérisé en ce que l'unité de commande et/ou de régulation (13, 14) place le procédé dans un état de sécurité, lorsque le facteur de compressibilité (z) du fluide à l'entrée dans la pompe centrifuge (11) n'a pas encore atteint son minimum.
  5. Procédé selon l'une quelconque des revendications 1 à 4, caractérisé en ce que l'état d'entrée du fluide est réglable avec des machines (1, 6) se présentant sous forme de compresseurs et/ou des appareils (3, 8) se présentant sous forme d'échangeurs de chaleur.
  6. Procédé selon la revendication 5, caractérisé en ce que le fluide à transporter traverse au moins un étage de compression et/ou un étage de refroidissement.
  7. Procédé pour séquestrer du dioxyde de carbone, dans lequel on porte le dioxyde de carbone à une pression et/ou une température appropriée pour un gisement prévu et on le transporte dans le gisement, caractérisé en ce qu'une pompe centrifuge (11) pompe le dioxyde de carbone dans le gisement conformément au procédé selon l'une quelconque des revendications 1 à 6, dans lequel des machines (1, 6) et/ou des appareils (3, 8) sont disposés avant la pompe centrifuge, lesquels influencent la pression et/ou la température du dioxyde de carbone, dans lequel on règle au moyen des machines (1, 6) et/ou des appareils (3, 8) l'état d'entrée du fluide, de telle manière que le fluide ne prenne dans la pompe centrifuge (11) que des états dans lesquels le facteur de compressibilité (z) du fluide a déjà atteint ou dépassé son minimum.
  8. Procédé selon la revendication 7, caractérisé en ce que le fluide se trouve à l'entrée dans la pompe centrifuge (11) et/ou dans la pompe centrifuge (11) dans un état hypercritique.
  9. Procédé selon la revendication 7 ou 8, caractérisé en ce que, lors d'une augmentation de la pression dans la pompe centrifuge (11), le facteur de compressibilité (z) du fluide reste constant ou augmente.
  10. Procédé selon l'une quelconque des revendications 7 à 9, caractérisé en ce que l'on mesure la température d'entrée (T) et/ou la pression d'entrée (p) du fluide et on la retransmet à une unité de commande et/ou de régulation (13, 14).
  11. Procédé selon la revendication 10, caractérisé en ce que l'unité de commande et/ou de régulation (13, 14) retransmet aux machines (1, 6) et/ou aux appareils (3, 8) des signaux par lesquels l'état d'entrée du fluide peut être réglé.
  12. Procédé selon la revendication 10 ou 11, caractérisé en ce que l'unité de commande et/ou de régulation (13, 14) déclenche une alarme, lorsque le facteur de compressibilité (z) du fluide à l'entrée dans la pompe centrifuge (11) n'a pas encore atteint son minimum.
  13. Procédé selon l'une quelconque des revendications 10 à 12, caractérisé en ce que l'unité de commande et/ou de régulation (13, 14) arrête l'installation, lorsque le facteur de compressibilité (z) du fluide à l'entrée de la pompe centrifuge (11) n'a pas encore atteint son minimum.
  14. Procédé selon l'une quelconque des revendications 7 à 13, caractérisé en ce que l'on règle l'état d'entrée du fluide avec des machines (1, 6) se présentant sous forme de compresseurs et/ou des appareils (3, 8) se présentant sous forme d'échangeurs de chaleur.
  15. Procédé selon la revendication 14, caractérisé en ce que le fluide à transporter traverse au moins un étage de compression (1, 6) et/ou un étage de refroidissement (3, 8).
EP10726092.9A 2009-06-30 2010-06-24 Dispositif de transport de fluides par des pompes centrifuges Active EP2449264B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
PL10726092T PL2449264T3 (pl) 2009-06-30 2010-06-24 Sposób przenoszenia płynów za pomocą pomp odśrodkowych

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102009031309A DE102009031309A1 (de) 2009-06-30 2009-06-30 Verfahren zur Förderung von Fluiden mit Kreiselpumpen
PCT/EP2010/058967 WO2011000761A1 (fr) 2009-06-30 2010-06-24 Dispositif de transport de fluides par des pompes centrifuges

Publications (2)

Publication Number Publication Date
EP2449264A1 EP2449264A1 (fr) 2012-05-09
EP2449264B1 true EP2449264B1 (fr) 2017-06-07

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US (1) US8449264B2 (fr)
EP (1) EP2449264B1 (fr)
JP (1) JP5738286B2 (fr)
CN (1) CN102575678B (fr)
BR (1) BRPI1008179B1 (fr)
DE (1) DE102009031309A1 (fr)
DK (1) DK2449264T3 (fr)
ES (1) ES2639405T3 (fr)
PL (1) PL2449264T3 (fr)
WO (1) WO2011000761A1 (fr)

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IT1398142B1 (it) * 2010-02-17 2013-02-14 Nuovo Pignone Spa Sistema singolo con compressore e pompa integrati e metodo.
EP2476476B1 (fr) 2011-01-14 2018-05-30 General Electric Technology GmbH Compression d'un fluide contenant du dioxyde de carbone
ITFI20110262A1 (it) * 2011-12-06 2013-06-07 Nuovo Pignone Spa "heat recovery in carbon dioxide compression and compression and liquefaction systems"
JP5995949B2 (ja) * 2014-12-19 2016-09-21 三菱重工業株式会社 多段圧縮機
US10718346B2 (en) * 2015-12-21 2020-07-21 General Electric Company Apparatus for pressurizing a fluid within a turbomachine and method of operating the same
ES2718742T3 (es) * 2016-02-19 2019-07-04 Linde Ag Procedimiento para la compresión gradual de un gas
FR3061240B1 (fr) * 2016-12-22 2019-05-31 Safran Aircraft Engines Procede ameliore de regulation d'un circuit d'alimentation
EP3686436A1 (fr) * 2019-07-31 2020-07-29 Sulzer Management AG Pompe à plusieurs étages et agencement de pompage sous-marin

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WO2009106160A1 (fr) 2008-02-25 2009-09-03 Siemens Aktiengesellschaft Procédé de compression de dioxyde de carbone ou d’un gaz ayant des propriétés analogues

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US8449264B2 (en) 2013-05-28
PL2449264T3 (pl) 2017-11-30
JP2012531551A (ja) 2012-12-10
CN102575678B (zh) 2015-08-19
EP2449264A1 (fr) 2012-05-09
BRPI1008179B1 (pt) 2020-06-23
DK2449264T3 (en) 2017-09-18
BRPI1008179A8 (pt) 2020-05-12
CN102575678A (zh) 2012-07-11
US20120111419A1 (en) 2012-05-10
ES2639405T3 (es) 2017-10-26
JP5738286B2 (ja) 2015-06-24
DE102009031309A1 (de) 2011-01-05
WO2011000761A1 (fr) 2011-01-06
BRPI1008179A2 (pt) 2016-03-01

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