EP3658816B1 - Installation de production de froid accouplée au dispositif de regasification d'un terminal de gaz naturel liquifié - Google Patents

Installation de production de froid accouplée au dispositif de regasification d'un terminal de gaz naturel liquifié Download PDF

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Publication number
EP3658816B1
EP3658816B1 EP17816399.4A EP17816399A EP3658816B1 EP 3658816 B1 EP3658816 B1 EP 3658816B1 EP 17816399 A EP17816399 A EP 17816399A EP 3658816 B1 EP3658816 B1 EP 3658816B1
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Prior art keywords
intermediate medium
refrigerating
lng
refrigerating agent
heat
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German (de)
English (en)
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EP3658816A1 (fr
Inventor
Rainer Braun
Peter Otto
Lothar BIHL
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Regascold GmbH
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Regascold GmbH
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C9/00—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure
    • F17C9/02—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure with change of state, e.g. vaporisation
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2221/00—Handled fluid, in particular type of fluid
    • F17C2221/01—Pure fluids
    • F17C2221/013—Carbone dioxide
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2221/00—Handled fluid, in particular type of fluid
    • F17C2221/03—Mixtures
    • F17C2221/032—Hydrocarbons
    • F17C2221/033—Methane, e.g. natural gas, CNG, LNG, GNL, GNC, PLNG
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2221/00—Handled fluid, in particular type of fluid
    • F17C2221/03—Mixtures
    • F17C2221/032—Hydrocarbons
    • F17C2221/035—Propane butane, e.g. LPG, GPL
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2223/00—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel
    • F17C2223/01—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel characterised by the phase
    • F17C2223/0107—Single phase
    • F17C2223/013—Single phase liquid
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2225/00—Handled fluid after transfer, i.e. state of fluid after transfer from the vessel
    • F17C2225/01—Handled fluid after transfer, i.e. state of fluid after transfer from the vessel characterised by the phase
    • F17C2225/0107—Single phase
    • F17C2225/0123—Single phase gaseous, e.g. CNG, GNC
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2227/00—Transfer of fluids, i.e. method or means for transferring the fluid; Heat exchange with the fluid
    • F17C2227/01—Propulsion of the fluid
    • F17C2227/0128—Propulsion of the fluid with pumps or compressors
    • F17C2227/0135—Pumps
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2227/00—Transfer of fluids, i.e. method or means for transferring the fluid; Heat exchange with the fluid
    • F17C2227/03—Heat exchange with the fluid
    • F17C2227/0302—Heat exchange with the fluid by heating
    • F17C2227/0309—Heat exchange with the fluid by heating using another fluid
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2227/00—Transfer of fluids, i.e. method or means for transferring the fluid; Heat exchange with the fluid
    • F17C2227/03—Heat exchange with the fluid
    • F17C2227/0302—Heat exchange with the fluid by heating
    • F17C2227/0309—Heat exchange with the fluid by heating using another fluid
    • F17C2227/0323—Heat exchange with the fluid by heating using another fluid in a closed loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2227/00—Transfer of fluids, i.e. method or means for transferring the fluid; Heat exchange with the fluid
    • F17C2227/03—Heat exchange with the fluid
    • F17C2227/0337—Heat exchange with the fluid by cooling
    • F17C2227/0341—Heat exchange with the fluid by cooling using another fluid
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2227/00—Transfer of fluids, i.e. method or means for transferring the fluid; Heat exchange with the fluid
    • F17C2227/03—Heat exchange with the fluid
    • F17C2227/0367—Localisation of heat exchange
    • F17C2227/0388—Localisation of heat exchange separate
    • F17C2227/0393—Localisation of heat exchange separate using a vaporiser
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2250/00—Accessories; Control means; Indicating, measuring or monitoring of parameters
    • F17C2250/03—Control means
    • F17C2250/032—Control means using computers
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2250/00—Accessories; Control means; Indicating, measuring or monitoring of parameters
    • F17C2250/04—Indicating or measuring of parameters as input values
    • F17C2250/0404—Parameters indicated or measured
    • F17C2250/043—Pressure
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2250/00—Accessories; Control means; Indicating, measuring or monitoring of parameters
    • F17C2250/04—Indicating or measuring of parameters as input values
    • F17C2250/0404—Parameters indicated or measured
    • F17C2250/0439—Temperature
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2250/00—Accessories; Control means; Indicating, measuring or monitoring of parameters
    • F17C2250/06—Controlling or regulating of parameters as output values
    • F17C2250/0605—Parameters
    • F17C2250/0626—Pressure
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2250/00—Accessories; Control means; Indicating, measuring or monitoring of parameters
    • F17C2250/06—Controlling or regulating of parameters as output values
    • F17C2250/0605—Parameters
    • F17C2250/0631—Temperature
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2265/00—Effects achieved by gas storage or gas handling
    • F17C2265/05—Regasification
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2270/00—Applications
    • F17C2270/01—Applications for fluid transport or storage
    • F17C2270/0102—Applications for fluid transport or storage on or in the water
    • F17C2270/0118—Offshore
    • F17C2270/0123—Terminals

Definitions

  • the invention relates to a system for supplying cold, which is coupled to the LNG (Liquefied Natural Gas) regasification device of an LNG terminal and which uses the high-quality, low-temperature cooling capacity available here.
  • LNG Liquified Natural Gas
  • Natural gas can be converted from the gaseous into the liquid phase under atmospheric pressure after cooling to -162 ° C and subsequent removal of the heat of condensation. This is associated with a reduction in volume to six hundredths of the value given at 1.013 bar and 15 ° C. Liquefied natural gas can thus be stored in an attractive way and transported over long distances.
  • the process chain to be implemented, which is both costly and value-adding, ranges from conveying and processing to liquefaction, storage, long-distance transport by tanker, renewed storage in large tanks and repeated transport to the user.
  • regasification which takes place in the area of the large tanks in so-called terminals, or at the user in so-called satellite systems.
  • the heat to be supplied during the regasification of LNG at a low temperature level has a high exergetic potential that can be used as a cooling capacity, but which remains almost completely unused worldwide.
  • the inventive task is to be seen in the development of equipment features in relation to a system for the safe supply of cold to both nearby and distant points of need, which is coupled to the LNG regasification facility of a large terminal, for example an LNG importing terminal, and in this way inexpensively substitutes the otherwise necessary, resource and environmentally polluting electrical energy consuming refrigeration.
  • the aim of the invention is to dissipate the heat required in LNG terminals for regasification of the LNG from available cooling demand points and thus to use it as valuable cooling capacity.
  • the prerequisite for this is the solution to two weighty problems.
  • large cooling capacities for example 1 MW, can be reliably and cost-effectively transported to nearby, distant and widely branched cooling demand points.
  • the low temperature level of the LNG which can be down to -162 ° C, places high demands on the cold toughness of the materials, on the control of large local and temporal temperature differences in the system components and on the flowability of the heat transfer fluid used as a coolant, which, however , one takes into account the cooling requirement that can be practically assigned to an LNG terminal, for example that of a cold store, which does not have to be temperature-controlled below -50 ° C.
  • CO 2 as the coolant, specifically in terms of its cooling by the heat transfer to the LNG and its heat absorption at the point of cold demand, exclusively in the state of a supercooled liquid.
  • this has the advantage of being much simpler to implement long refrigerant transport routes and thus also the advantage of more cost-effective system technology.
  • the lowest permissible temperature of the refrigerant CO 2 in a closed circuit is set at -50 ° C in view of its triple point coordinates 5.19 bar and -56.6 ° C, which on the one hand provides sufficient security against the formation of a solid phase, and on the other hand with regard to the Cold supply offers a sufficiently low temperature level.
  • the necessary compliance with this temperature value is ensured by diversely redundant system and control measures.
  • Liquid CO 2 for example in a state of -50 ° C and 10.0 bar, has very good physical properties of density, specific heat capacity, thermal conductivity and viscosity, so that correspondingly effective heat transfers result and the circulation in the refrigerant circuit requires only a low pumping capacity.
  • Other important advantages of CO 2 are: It is chemically inactive, non-corrosive, non-flammable and overall environmentally friendly. This is the reason why the cold supply coupled to the regasification device of the LNG terminal can provide the cold much more cost-effectively than the conventional electrically driven compressor refrigeration machine.
  • the primary use of the intermediate medium propane which in a closed circuit by natural circulation at a safe average temperature level in an intermediate medium evaporator, takes over the heat from the refrigerant in order to then transfer them to the LNG in an intermediate medium condenser.
  • two horizontally aligned, horizontally aligned, tube bundle heat exchangers are used, in whose tubes the coolant gives off its heat or the LNG absorbs the heat, and between which the phases in equilibrium, propane as saturated steam and propane in the boiling state, are used to ensure the natural circulation, separated and transported in generously dimensioned lines with minimal pressure loss.
  • Pressure monitoring of the intermediate medium is used to keep the temperature in the boiling and condensing propane constant at a safe medium level. Its pressure is regulated to a target value of 0.611 bar with the help of a computer-aided system control and an LNG throttle valve, which as an actuator determines the LNG flow and thus the heat transfer in the intermediate medium condenser, which correlates with the temperature -55 ° C according to the propane vapor pressure curve .
  • the detection of the pressure of the intermediate medium also serves to safeguard against a possible leak in the heat transfer system refrigerant - intermediate medium evaporator - propane connection lines - intermediate medium condenser - LNG.
  • a safety device is available that detects any leakage from the pipes transporting LNG or CO 2 into the spaces containing the intermediate medium propane, namely into the shell spaces of the two tube bundle heat exchangers and into the propane connection lines .
  • the supercooled CO 2 is circulated by means of a refrigerant pump in a closed circuit consisting of well-insulated pipelines, where it cools down to -50 ° C in the intermediate medium evaporator while releasing heat to the intermediate medium, then in a supercooled state it reaches the cold demand point to be supplied, possibly remote, in order to be heated up to near the boiling point by absorbing heat, which corresponds to the cooling capacity, and then to be fed to a coolant collector and separator. In this collector and separator, phase equilibrium is finally achieved between the refrigerant condensate and saturated refrigerant vapor, for example at -40 ° C and 10.0 bar.
  • the coolant condensate then flows as a return over an appropriate inlet height to prevent cavitation to the coolant pump, which conveys it to the intermediate medium evaporator, in which the heat is absorbed by the intermediate medium evaporating here, which circulates naturally to the intermediate medium condenser and condenses there and transfers the heat to the LNG to be regasified.
  • the cooling supply system coupled to the regasification facility of an LNG terminal uses the heat required for regasification of the LNG as cooling capacity. This is transferred with the help of a coolant (1), which is circulated with a coolant pump (7) in a closed circuit consisting of well-insulated pipes (8), to the possibly remote cold demand point (2).
  • the coolant (1) is liquid CO 2 , which is cooled in the tubes of a tube bundle heat exchanger, the so-called intermediate medium evaporator (4) to the permissible minimum value -50 ° C, then reaches the cold demand point (2) to be supplied in a supercooled state there by heat absorption, which corresponds to the cooling capacity, to be heated up to the vicinity of the boiling state.
  • the next station in the circuit is the refrigerant collector and separator (9), in which the phase equilibrium between refrigerant condensate (10) and saturated refrigerant vapor (11), which determines the pressure in the circulatory system, is achieved.
  • the coolant condensate (10) then flows through an appropriate inlet head that prevents cavitation to the coolant pump (7), which conveys it as a return to the intermediate medium evaporator (4).
  • the intermediate medium evaporator (4) In the intermediate medium evaporator (4), the heat given off by the intermediate medium (12) propane, which is boiling in the shell space, is absorbed by the heat transferring medium (1) flowing in the tubes. The evaporated intermediate medium (12) then leaves the upper area of the shell space of the intermediate medium evaporator (4) via an intermediate medium saturated steam line (13) and arrives in the upper shell area of a further tube bundle heat exchanger, the so-called intermediate medium condenser (5), which is arranged above the intermediate medium evaporator (4) and how this is aligned horizontally.
  • the intermediate medium condensing in the jacket space of the intermediate medium condenser (5) finally supplies the heat that is required for regasification of the LNG flowing in the pipes, and then flows from the lower jacket space area of the intermediate medium condenser (5) via the intermediate medium condensate line (14) down to the lower jacket space area of the intermediate medium evaporator (4).
  • the heat transfer from the refrigerant (1) to the LNG, created with the intermediate medium (12) takes place in natural circulation, that is, in free convection without a circulation pump, and at a safe average temperature level, which excludes the risk of the refrigerant (1) solidifying.
  • the natural circulation of the evaporating and condensing intermediate medium (12) propane between the two tube bundle heat exchangers, the intermediate medium evaporator (4) and the intermediate medium condenser (5) is achieved through the generously dimensioned intermediate medium saturated steam line (13) and the intermediate medium condensate line (14), which have minimal pressure losses and condensate separately and, if necessary, also convey in several parallel lines.
  • the refrigeration supply system shown contains several measures to ensure a trouble-free refrigeration supply that complies with the specified operating data.
  • An intermediate medium pressure control and monitoring (17) is used to keep the temperature of the boiling and condensing intermediate medium (12) propane in the intermediate medium evaporator (4) and in the intermediate medium condenser (5) constant at a safe medium level.
  • the measured pressure of the intermediate medium (12), which is in phase equilibrium, is determined with the aid of a computer-aided system control (20) and an LNG throttle valve (16) which, as an actuator, determines the LNG flow rate (3) and thus the heat transfer in the intermediate medium condenser (5), Regulated to a setpoint, for example 0.611 bar, which correlates with the temperature -55 ° C according to the propane vapor pressure curve.
  • the fact that the secondary medium (1) cools down as deeply as possible due to the transfer of heat to the intermediate medium (12), but not below the minimum permissible value of -50 ° C, is also achieved in a diversely redundant manner with the secondary medium outlet temperature control (15).
  • the temperature of the refrigerant (1) is measured at the point of deepest cooling, that is, at the outlet of the intermediate medium evaporator (4).
  • regulation takes place with the help of the system control (20) and the LNG throttle valve (16), which, as an actuator, determines the LNG flow rate (3) and thus the cooling of the refrigerant (1) resulting from the heat transfer to the LNG.
  • the detection of the pressure of the intermediate medium (12) also serves to protect against a possible leak in the heat transfer system refrigerant - intermediate medium evaporator - propane connection lines - intermediate medium condenser - LNG.
  • intermediate medium pressure regulation and monitoring (17), computer-aided system control (20) and LNG throttle valve (16) a safety device is available that prevents any leakage from the pipes transporting LNG or CO 2 into the intermediate medium (12) propane contained spaces detected, namely in the shell spaces of the two tube bundle heat exchangers, the intermediate medium evaporator (4) and the intermediate medium condenser (5), as well as in the propane connection lines, the intermediate medium saturated steam line (13) and the
  • the level of the ascertained pressure increase can also be used to identify whether the leak concerns penetrating LNG, which is usually pumped to the high, mostly supercritical pressure required for natural gas use before regasification, or penetrating CO 2 , its pressure despite the state of a supercooled liquid is significantly lower.
  • VKM compressor refrigeration machine
  • the replacement refrigeration system (6), the refrigerant separator pressure control (21), the computer-aided system control (20), the disconnectable refrigerant pump (7) and the LNG throttle valve (16) form a safety system that prevents the pressure in the refrigerant circuit from falling possible interruption of the LNG flow (3) and / or if the heat supply in the cooling demand point (2) exceeds the specified limits, for example 25 bar, the steam pressure at -12 ° C, and therefore a safety valve is actuated must become.

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Filling Or Discharging Of Gas Storage Vessels (AREA)

Claims (7)

  1. Installation d'alimentation en froid pouvant être couplée au dispositif de regazéification d'un terminal de gaz naturel liquéfié et destinée à l'utilisation de la puissance frigorifique de haute valeur disponible à un faible niveau de température dans la regazéification de GNL, caractérisée en ce que, entre une entrée de GNL (3) et un point de demande de froid (2), sont aménagés les composants essentiels au fonctionnement suivants et se trouvant en liaison active entre eux, à savoir un condensateur de fluide intermédiaire (5), un évaporateur de fluide intermédiaire (4), un collecteur et un séparateur de frigoporteur (9) pour du condensat frigoporteur (10) et de la vapeur saturée frigoporteur (11), une installation frigorifique de remplacement (6), une pompe frigoporteur (7), une vanne d'étranglement GNL (16) et une commande d'installation assistée par ordinateur (20), composants qui, en utilisant du propane comme fluide intermédiaire (12), coopèrent de sorte que du liquide frigoporteur surrefroidi (1) peut être circulé au moyen de la pompe frigoporteur (7) dans un circuit fermé existant composé par des tuyauteries (8) bien isolées en se refroidissant jusqu'à -50°C dans l'évaporateur de fluide intermédiaire (4) en dégageant de la chaleur au fluide intermédiaire (12) avant d'arriver, en état surrefroidi, jusqu'au point de demande de froid (2) à être alimenté et se trouvant, le cas échéant, en situation éloignée, afin de se réchauffer ici par absorption thermique, ce qui correspond à la puissance frigorifique, jusqu'à un niveau proche de l'état d'ébullition, pouvant être amené, par la suite, à un collecteur et séparateur de frigoporteur (9) dans lequel un équilibre des phases est finalement atteint entre le condensat frigoporteur (10) et la vapeur saturée de frigoporteur (11), le condensat frigoporteur (10) étant ramené, comme flux de retour, à l'évaporateur de fluide intermédiaire (4) dans lequel la chaleur est absorbée par le fluide intermédiaire (12) s'évaporant ici et arrive après, par circulation naturelle, au condensateur de fluide intermédiaire (5) afin de transmettre, en condensant à cet endroit, la chaleur au GNL à être regazéifié,
    en ce que, en outre, une sécurité d'approvisionnement est atteinte, grâce aux équipements de réglage qui évitent le dépassement négatif de la température minimale admissible du frigoporteur et, de plus, grâce à l'installation frigorifique de remplacement (6) qui est couplée au collecteur et séparateur de frigoporteur (9) et évite une augmentation de la pression inadmissible dans le circuit frigoporteur et causée par l'interruption du débit de GNL (3) et/ou par un apport de chaleur dépassant les limites prévues au point de demande de froid (2).
  2. Installation d'alimentation en froid selon la revendication 1, caractérisée en ce que du CO2 est utilisé comme frigoporteur (1) et ceci de sorte que celui-ci transporte la puissance frigorifique sans changement de phase, en l'état liquide et surrefroidi, au point de demande de froid (2) à être alimenté, permettant de couvrir, de manière économique, même des grandes distances, en maîtrisant le risque de solidification du CO2, dont le point triple a les coordonnées de 5,19 bars et de -56,6°C, grâce à la limitation du refroidissement à une valeur minimale de -50 °C, qui est assurée par la commande assistée par ordinateur de l'installation (20) qui utilise comme actionneur la vanne d'étranglement de GNL (16) et comme paramètre de réglage la température du frigoporteur enregistrée par le dispositif de réglage de température (15) à la sortie de l'évaporateur du fluide intermédiaire (4) où elle atteint sa valeur la plus faible.
  3. Installation d'alimentation en froid selon les revendications 1 et 2, caractérisée en ce que, afin de prévenir le risque de solidification du frigoporteur (1), la transmission de chaleur se fait à l'aide de propane comme fluide intermédiaire (12) qui absorbe, en circulation naturelle sans pompe de circulation et d'abord à un niveau moyen sûr de température, le flux thermique dégagé par le frigoporteur (1) afin de le transmettre, par la suite, au GNL, ce qui est assuré grâce à l'aménagement d'un condensateur de fluide intermédiaire (5) au-dessus d'un évaporateur de fluide intermédiaire (4) et à ce que les deux sont des échangeurs de chaleur à faisceaux tubulaires alignés horizontalement et convenants aux températures profondes à être maîtrisées, à savoir l'évaporateur de fluide intermédiaire (4) qui conduit le frigoporteur (1) par les tubes tandis que le fluide intermédiaire (12) est en ébullition dans l'espace compris entre les tubes et la calandre, et le condensateur de fluide intermédiaire (5) qui mène le GNL dans les tubes, tandis que le fluide intermédiaire (12) condense dans le espace compris entre les tubes et la calandre, les transports des phases gazeuse et liquide étant réalisés, afin d'assurer la circulation naturelle, de manière séparée et avec des pertes de pression minimales dans des tuyaux généreusement dimensionnés, à savoir dans la conduite de vapeur saturée de fluide intermédiaire (13) et dans la conduite de condensat de fluide intermédiaire (14), chaque fois dans une ou dans plusieurs conduites parallèles qui mènent la vapeur de l'espace supérieur compris entre les tubes et la calandre de l'évaporateur de fluide intermédiaire (4) à l'espace supérieur compris entre les tubes et la calandre du condensateur de fluide intermédiaire (5) et qui mènent le condensat au moins par une conduite de condensat de fluide intermédiaire (14) de l'espace inférieur compris entre les tubes et la calandre du condensateur de fluide intermédiaire (5) à l'espace inférieur compris entre les tubes et la calandre de l'évaporateur de fluide intermédiaire (4).
  4. Installation d'alimentation en froid selon au moins une des revendications susmentionnées, caractérisée en ce que, à l'aide d'un dispositif de réglage et de surveillance de la pression de fluide intermédiaire (17) dans le propane, fluide intermédiaire (12), d'une commande d'installation assistée par ordinateur (20) et d'une vanne d'étranglement de GNL (16), il est assuré par des techniques de réglage diversitaires redondantes que le frigoporteur (1), à savoir 002, se refroidi dans l'évaporateur de fluide intermédiaire (4) jusqu'à la température la plus basse possible mais non plus bas que -50°C et ne passe donc pas à la phase solide, en utilisant comme variable commandée la pression de propane dont la valeur de consigne minimale admissible est définie comme la valeur minimale admissible de 0,611 bar de propane se trouvant en équilibre de phases en état de d'ébullition et de condensation, ce qui, selon la courbe de pression de vapeur du propane est en corrélation avec la température de - 55 °C dont l'atteinte dépend du transfert de chaleur au GNL donc de son débit qui est ajustable au moyen de la vanne d'étranglement de GNL (16).
  5. Installation d'alimentation en froid selon au moins une des revendications susmentionnées, caractérisée en ce qu'un dispositif technique de sécurité destinée à la surveillance et au réglage de la pression du fluide intermédiaire (12) et comprenant comme composants le réglage et la surveillance de la pression du fluide intermédiaire(17), la commande assistée par ordinateur de l'installation (20) et la vanne d'étranglement de GNL (16), est mis en place ce qui permet de détecter une éventuelle fuite des tuyaux transportant du GNL ou du CO2 dans l'espace contenant le fluide intermédiaire (12) et d'interrompre, comme contre-mesure, l'alimentation en GNL et le fonctionnement de la pompe frigoporteur (7), l'importance de l'augmentation de pression détectée permettant d'identifier en plus si la fuite concerne du GNL entrant qui, habituellement, vient d'être pompé à la pression élevée et souvent surcritique nécessaire aux fins de l'utilisation de gaz naturel avant la regazéification, ou bien du CO2 entrant dont la pression, en dépit de son état de liquide surrefroidi, est nettement moins élevée.
  6. Installation d'alimentation en froid selon la revendication 1, caractérisée en ce qu'une machine frigorifique à compression (VKM) conventionnelle est mise en place, comme installation frigorifique de remplacement (6), au-dessus du collecteur et du séparateur de frigoporteur (9), et intégrée, en utilisant ce dernier comme accouplement, au système frigoporteur, de la vapeur saturée de frigoporteur (11), affluent en convection libre et en circulation naturelle par la conduite de vapeur saturée frigoporteur (18), condensant à l'évaporateur dessiné, comme d'habitude, comme échangeur de chaleur par surface de la machine frigorifique à compression (VKM) avant de s'écouler de retour en passant par la conduite de condensat frigoporteur (19), de sorte que, à l'aide de la puissance frigorifique de l'installation frigorifique de remplacement (6), un double effet soit atteignable, permettant, à savoir d'une part, à la vapeur saturée de frigoporteur (10) ainsi générée d'être reliquéfiée et d'être accumulée dans le collecteur et séparateur de frigoporteur (9) et d'autre part, de réduire la pression dans le circuit frigoporteur, ce qui, à l'aide du dispositif technique sécurité constitué par l'installation frigorifique de remplacement (6), par le dispositif de réglage de pression du séparateur de frigoporteur (21), par la commande d'installation assistée par ordinateur (20), par la vanne d'étranglement de GNL (16) et par la pompe frigoporteur (7) déconnectable, permet d'éviter, en cas d'une éventuelle interruption du débit de GNL (3) et/ou d'un apport de chaleur dépassant les limites prévues au point de demande de froid (2), l'augmentation inadmissible de la pression du frigoporteur.
  7. Installation d'alimentation en froid selon au moins une des revendications susmentionnées, caractérisée en ce que le point de demande de froid (2) se trouve en dehors des autres composants de l'installation.
EP17816399.4A 2017-07-25 2017-10-19 Installation de production de froid accouplée au dispositif de regasification d'un terminal de gaz naturel liquifié Active EP3658816B1 (fr)

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DE102017007009.1A DE102017007009A1 (de) 2017-07-25 2017-07-25 Kälteversorgungsanlage, gekoppelt an die Regasifizierungseinrichtung eines Liquified Natural Gas Terminals
PCT/DE2017/000352 WO2019020135A1 (fr) 2017-07-25 2017-10-19 Installation de production de froid accouplée au dispositif de regasification d'un terminal de gaz naturel liquifié

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CN110345386A (zh) * 2019-07-19 2019-10-18 中冶焦耐(大连)工程技术有限公司 一种自循环式的lng管道预冷工艺
DE102020001338A1 (de) 2020-02-29 2021-09-02 REGASCOLD GmbH Wärmeübertrager für die Rückgewinnung von Kälteleistung aus der Regasifizierung tiefkalter verflüssigter Gase

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JPS535207A (en) 1976-07-05 1978-01-18 Osaka Gas Co Ltd Vaporizer of liquefied natural gas
DE3035349C2 (de) 1980-09-19 1985-06-27 Uhde Gmbh, 4600 Dortmund Anlage zur Verdampfung von flüssigem Erdgas
JP3946398B2 (ja) 2000-01-18 2007-07-18 株式会社神戸製鋼所 中間媒体式気化器及び当該気化器を用いた天然ガスの供給方法
JP5426374B2 (ja) * 2006-07-25 2014-02-26 シエル・インターナシヨネイル・リサーチ・マーチヤツピイ・ベー・ウイ 液体流を気化するための方法及び装置
FR2931222B1 (fr) * 2008-05-16 2014-02-21 Batignolles Tech Therm Systeme et procede de vaporisation d'un fluide cryogenique, notamment du gaz naturel liquefie, a base de co2
DE202015008836U1 (de) 2015-12-28 2016-02-25 Eco ice Kälte GmbH Wärmeaustauscher zur Rückgewinnung von Kälte bei der Regasifizierung tiefkalter Flüssigkeiten
DE102016006121A1 (de) 2015-12-28 2017-06-29 Eco ice Kälte GmbH Verfahren und Wärmeaustauscher zur Rückgewinnung von Kälte bei der Regasifizierung tiefkalter Flüssigkeiten

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WO2019020135A1 (fr) 2019-01-31
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DE102017007009A1 (de) 2019-01-31
EP3658816A1 (fr) 2020-06-03

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