WO2013146316A1 - 船舶、液化ガス蒸発装置およびその制御方法ならびにその改修方法 - Google Patents
船舶、液化ガス蒸発装置およびその制御方法ならびにその改修方法 Download PDFInfo
- Publication number
- WO2013146316A1 WO2013146316A1 PCT/JP2013/057269 JP2013057269W WO2013146316A1 WO 2013146316 A1 WO2013146316 A1 WO 2013146316A1 JP 2013057269 W JP2013057269 W JP 2013057269W WO 2013146316 A1 WO2013146316 A1 WO 2013146316A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- liquefied gas
- gas
- pipe
- flow rate
- main pipe
- Prior art date
Links
Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B63—SHIPS OR OTHER WATERBORNE VESSELS; RELATED EQUIPMENT
- B63B—SHIPS OR OTHER WATERBORNE VESSELS; EQUIPMENT FOR SHIPPING
- B63B25/00—Load-accommodating arrangements, e.g. stowing, trimming; Vessels characterised thereby
- B63B25/02—Load-accommodating arrangements, e.g. stowing, trimming; Vessels characterised thereby for bulk goods
- B63B25/08—Load-accommodating arrangements, e.g. stowing, trimming; Vessels characterised thereby for bulk goods fluid
- B63B25/12—Load-accommodating arrangements, e.g. stowing, trimming; Vessels characterised thereby for bulk goods fluid closed
- B63B25/16—Load-accommodating arrangements, e.g. stowing, trimming; Vessels characterised thereby for bulk goods fluid closed heat-insulated
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B63—SHIPS OR OTHER WATERBORNE VESSELS; RELATED EQUIPMENT
- B63H—MARINE PROPULSION OR STEERING
- B63H21/00—Use of propulsion power plant or units on vessels
- B63H21/38—Apparatus or methods specially adapted for use on marine vessels, for handling power plant or unit liquids, e.g. lubricants, coolants, fuels or the like
-
- 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
-
- G—PHYSICS
- G01—MEASURING; TESTING
- G01F—MEASURING VOLUME, VOLUME FLOW, MASS FLOW OR LIQUID LEVEL; METERING BY VOLUME
- G01F5/00—Measuring a proportion of the volume flow
-
- G—PHYSICS
- G05—CONTROLLING; REGULATING
- G05D—SYSTEMS FOR CONTROLLING OR REGULATING NON-ELECTRIC VARIABLES
- G05D7/00—Control of flow
- G05D7/06—Control of flow characterised by the use of electric means
- G05D7/0617—Control of flow characterised by the use of electric means specially adapted for fluid materials
- G05D7/0629—Control of flow characterised by the use of electric means specially adapted for fluid materials characterised by the type of regulator means
- G05D7/0635—Control of flow characterised by the use of electric means specially adapted for fluid materials characterised by the type of regulator means by action on throttling means
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B63—SHIPS OR OTHER WATERBORNE VESSELS; RELATED EQUIPMENT
- B63H—MARINE PROPULSION OR STEERING
- B63H21/00—Use of propulsion power plant or units on vessels
- B63H21/12—Use of propulsion power plant or units on vessels the vessels being motor-driven
- B63H21/14—Use of propulsion power plant or units on vessels the vessels being motor-driven relating to internal-combustion engines
-
- 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
- F17C2223/0146—Two-phase
- F17C2223/0153—Liquefied gas, 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
- F17C2223/0146—Two-phase
- F17C2223/0153—Liquefied gas, e.g. LPG, GPL
- F17C2223/0161—Liquefied gas, e.g. LPG, GPL cryogenic, e.g. LNG, GNL, 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
- F17C2223/00—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel
- F17C2223/03—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel characterised by the pressure level
- F17C2223/033—Small pressure, e.g. for liquefied gas
-
- 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
- F17C2223/04—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel characterised by other properties of handled fluid before transfer
- F17C2223/042—Localisation of the removal point
- F17C2223/046—Localisation of the removal point in the 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
- F17C2225/00—Handled fluid after transfer, i.e. state of fluid after transfer from the vessel
- F17C2225/03—Handled fluid after transfer, i.e. state of fluid after transfer from the vessel characterised by the pressure level
- F17C2225/033—Small pressure, e.g. for liquefied gas
-
- 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
- F17C2227/0114—Propulsion of the fluid with vacuum injectors, e.g. venturi
-
- 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
-
- 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
- F17C2250/04—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
- F17C2250/04—Indicating or measuring of parameters as input values
- F17C2250/0404—Parameters indicated or measured
- F17C2250/0443—Flow or movement of content
-
- 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
- F17C2250/00—Accessories; Control means; Indicating, measuring or monitoring of parameters
- F17C2250/06—Controlling or regulating of parameters as output values
- F17C2250/0605—Parameters
- F17C2250/0636—Flow or movement of content
-
- 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
- F17C2260/00—Purposes of gas storage and gas handling
- F17C2260/02—Improving properties related to fluid or fluid transfer
- F17C2260/024—Improving metering
-
- 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
- F17C2265/06—Fluid distribution
- F17C2265/066—Fluid distribution for feeding engines for propulsion
-
- 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
- F17C2270/0105—Ships
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02T—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO TRANSPORTATION
- Y02T70/00—Maritime or waterways transport
- Y02T70/50—Measures to reduce greenhouse gas emissions related to the propulsion system
- Y02T70/5218—Less carbon-intensive fuels, e.g. natural gas, biofuels
Definitions
- the present invention relates to a ship equipped with a liquefied gas storage tank, a liquefied gas evaporation apparatus, a control method thereof, and a repair method thereof.
- an LNG vaporizer that guides and evaporates LNG in the LNG tank as shown in Patent Document 1 below.
- An LNG ship equipped with a large LNG vaporizer and a small LNG vaporizer for generating fuel gas is also well known.
- the installation of one large LNG vaporizer and one small LNG vaporizer increases the installation space and increases the initial investment. Therefore, it is preferable that the large LNG vaporizer is also used as the small LNG vaporizer.
- the LNG vaporizer generally employs a steam-heated shell and tube heat exchanger, LNG is passed through the tube side, and the shell side is a saturated steam atmosphere.
- the heated LNG exits the heat exchanger in the superheated gas state, and adjusts the outlet temperature by bypassing a part of the LNG at the heat exchanger inlet and spraying the superheated gas state gas. Yes.
- the amount of evaporative gas is controlled according to the set value based on the mass flow rate after measuring the volume flow rate with an orifice flow meter or a venturi flow meter installed in the outlet pipe and converting it to a mass flow rate.
- a flow rate adjustment valve is provided in the LNG line on the heat exchanger inlet side, and a temperature adjustment valve is provided in the LNG line of the temperature adjustment bypass flow path.
- These flow rate adjustment valve and temperature adjustment valve are designed and sized according to the rated flow rate, so that when a very small amount of LNG is allowed to pass, sufficient LNG flow rate adjustment function and gas temperature adjustment function cannot be exhibited. .
- the gas flow rate is not accurately detected by a flow meter, making it difficult to manage the amount of evaporation.
- the LNG line 102 on the inlet side of the LNG vaporizer 101 is provided with a flow rate adjusting valve 103 for high flow rate and a flow rate adjusting valve 104 for low flow rate in parallel.
- a temperature adjustment valve 106 for high flow rate and a temperature adjustment valve 107 for low flow rate are provided in parallel in a temperature adjustment bypass LNG line 108 for spraying LNG to the temperature adjustment slow heat device 105.
- the flow rate adjustment valve and the temperature adjustment valve are configured separately for the high flow rate and the low flow rate, a wide flow range can be handled.
- the flow rate is measured by the flow meter 109 on the outlet side of the heat sink 105, there is still room for improvement in the flow rate measurement accuracy at a low flow rate.
- the present invention has been made in view of such circumstances, and includes a ship equipped with a liquefied gas evaporation device that can accurately control the flow rate or control the temperature even if the flow rate range is wide, a liquefied gas evaporation device, and a control method thereof. It aims at providing the repair method.
- the ship, the liquefied gas evaporation apparatus, the control method thereof, and the repair method thereof according to the present invention employ the following means. That is, the ship according to the first aspect of the present invention is a liquefied gas main pipe that guides liquefied gas, an evaporator that evaporates the liquefied gas guided from the liquefied gas main pipe, and is vaporized by the evaporator.
- a gas outlet pipe for guiding gas; a gas flow meter provided in the gas outlet pipe; a flow rate adjusting valve provided in the liquefied gas main pipe for adjusting a liquefied gas flow rate leading to the evaporator; and the flow rate adjusting valve A control unit that controls the liquefied gas main pipe, bypassing the liquefied gas main pipe, bypassing the liquefied gas main pipe, and re-merging with the liquefied gas main pipe.
- a gas sub-pipe a switching valve for switching between the liquefied gas main pipe and the liquefied gas sub-pipe, a liquid flow meter for measuring the flow rate of the liquefied gas flowing through the liquefied gas sub-pipe, and liquefaction flowing through the liquefied gas sub-pipe Depressurization hand depressurizing gas
- the control unit controls the flow rate adjusting valve based on a measurement value of the gas flow meter
- the said flow control valve is controlled based on the measured value of the said liquid flow meter, and liquefied fuel gas is supplied from the said liquefied gas evaporation apparatus It has a main machine.
- the liquefied gas flows at a high flow rate when the liquefied gas main piping is selected by the switching valve, and flows at a low flow rate when the liquefied gas sub piping is selected.
- the flow rate adjusting valve is controlled based on the measured value of the gas flow meter provided in the gas outlet pipe on the downstream side of the evaporator. Thereby, the gas of desired flow rate can be supplied accurately.
- the flow rate adjustment valve is controlled based on the measured value of the liquid flow meter that measures the flow rate of the liquefied gas flowing through the liquefied gas sub-pipe. That is, in the case of a low flow rate, the measured value of the gas flow meter is not used. This is because the gas flowmeter is used when a high flow rate flows, so that measurement accuracy at a low flow rate cannot be guaranteed. Therefore, it was decided to measure the flow rate of the liquefied gas flowing through the liquefied gas auxiliary pipe with a liquid flow meter with high accuracy.
- the liquefied gas flowing through the liquefied gas sub-pipe is decompressed by the decompression means, so that the opening range of the flow rate adjusting valve can be increased compared to when the pressure is not decompressed.
- the opening range of the flow rate adjusting valve can be increased compared to when the pressure is not decompressed.
- the liquefied gas evaporation apparatus includes a liquefied gas main pipe that guides the liquefied gas, an evaporator that evaporates the liquefied gas guided from the liquefied gas main pipe, and the evaporator A gas outlet pipe for leading the vaporized gas; a gas flow meter provided in the gas outlet pipe; a flow rate adjusting valve provided in the liquefied gas main pipe for adjusting a liquefied gas flow quantity leading to the evaporator; A control unit that controls a flow rate adjusting valve, and a liquefied gas that is branched from the liquefied gas main pipe, bypasses, and rejoins the liquefied gas main pipe, and has a lower flow rate than the liquefied gas main pipe A liquefied gas sub-pipe through which the gas flows, a switching valve for switching between the liquefied gas main pipe and the liquefied gas sub-pipe, a liquid flow meter for measuring the flow rate of
- the liquefied gas flows at a high flow rate when the liquefied gas main piping is selected by the switching valve, and flows at a low flow rate when the liquefied gas sub piping is selected.
- the flow rate adjusting valve is controlled based on the measured value of the gas flow meter provided in the gas outlet pipe on the downstream side of the evaporator. Thereby, the gas of desired flow rate can be supplied accurately.
- the flow rate adjustment valve is controlled based on the measured value of the liquid flow meter that measures the flow rate of the liquefied gas flowing through the liquefied gas sub-pipe. That is, in the case of a low flow rate, the measured value of the gas flow meter is not used. This is because the gas flowmeter is used when a high flow rate flows, so that measurement accuracy at a low flow rate cannot be guaranteed. Therefore, it was decided to measure the flow rate of the liquefied gas flowing through the liquefied gas auxiliary pipe with a liquid flow meter with high accuracy.
- the liquefied gas flowing through the liquefied gas sub-pipe is decompressed by the decompression means, so that the opening range of the flow rate adjusting valve can be increased compared to when the pressure is not decompressed.
- the opening range of the flow rate adjusting valve can be increased compared to when the pressure is not decompressed.
- the liquefied gas evaporation apparatus concerning the 3rd aspect of this invention is provided in the said gas outlet piping, the temperature regulator which adjusts gas temperature by spraying liquefied gas, and the downstream of the said liquefied gas auxiliary piping
- a temperature control pipe for introducing a part of the liquefied gas from the liquefied gas main pipe at a position and spraying the liquefied gas to the temperature regulator, a temperature control valve provided in the temperature control pipe, and a temperature control valve.
- a temperature sensor for measuring the temperature of the gas, wherein the control unit controls the temperature control valve based on a measurement value of the temperature sensor.
- the temperature control valve is also provided with a low flow rate, even when the flow rate is high, since the liquefied gas decompressed by the decompression means is guided when the flow rate is low, as with the flow rate adjustment valve described above. Even in this case, the temperature control valve can be controlled in an opening range with good controllability.
- a gas-liquid separator is provided in the liquefied gas main pipe at the downstream position of the liquefied gas sub pipe and at the upstream position of the flow regulating valve. Is provided.
- the liquefied gas that has been depressurized through the depressurizing means of the liquefied gas sub-pipe may become a gas-liquid two-phase flow containing flash gas.
- the gas phase portion obstructs the flow of the liquid phase in the flow rate adjusting valve. Therefore, in the present invention, only the liquid phase is guided to the flow rate adjusting valve by providing a gas-liquid separator on the upstream side of the flow rate adjusting valve.
- the liquefied gas evaporator according to the fifth aspect of the present invention includes a gas vent pipe that guides the gas separated by the gas-liquid separator to the gas outlet pipe, and a gas flow rate provided in the gas vent pipe.
- An adjustment valve, and the control unit controls the gas flow rate adjustment valve based on a measurement value of the temperature sensor.
- the gas separated by the gas-liquid separator is flow-adjusted by the gas flow regulating valve and then led to the gas outlet pipe. Thereby, adjustment of the gas temperature which flows through gas outlet piping can be performed.
- control method of the liquefied gas evaporation apparatus includes a liquefied gas main pipe that leads the liquefied gas, an evaporator that evaporates the liquefied gas led from the liquefied gas main pipe, and the evaporation A gas outlet pipe for leading the gas vaporized in the evaporator, a gas flow meter provided in the gas outlet pipe, and a flow rate adjusting valve provided in the liquefied gas main pipe for adjusting the flow rate of the liquefied gas led to the evaporator And a control unit for controlling the flow rate adjusting valve, and a bypass branching off from the liquefied gas main pipe and rejoining the liquefied gas main pipe, and having a lower flow rate than the liquefied gas main pipe.
- a liquefied gas sub-pipe through which the liquefied gas flows a switching valve for switching between the liquefied gas main pipe and the liquefied gas sub-pipe, a liquid flow meter for measuring the flow rate of the liquefied gas flowing through the liquefied gas sub-pipe, and the liquefying Liquefaction flowing in the gas sub-pipe
- a depressurizing means for depressurizing the gas, and when the liquefied gas main pipe is selected by the switching valve by the control unit, the measured value of the gas flow meter
- the flow rate adjusting valve is controlled based on the measured value of the liquid flow meter.
- a method for refurbishing a liquefied gas evaporation apparatus includes a liquefied gas main pipe that leads liquefied gas, an evaporator that evaporates the liquefied gas led from the liquefied gas main pipe, and the evaporation A gas outlet pipe for leading the gas vaporized in the evaporator, a gas flow meter provided in the gas outlet pipe, and a flow rate adjusting valve provided in the liquefied gas main pipe for adjusting the flow rate of the liquefied gas led to the evaporator And a control method for controlling the flow rate adjusting valve, the method for refurbishing the liquefied gas evaporator, wherein the liquefied gas main pipe is branched and bypassed to rejoin the liquefied gas main pipe A liquefied gas sub-pipe through which a liquefied gas whose flow rate is lower than that of the liquefied gas main pipe, a switching valve for switching between the liquefied gas
- a liquefied gas sub-pipe, a liquid flow meter, and a pressure reducing means are additionally provided, and the liquefied gas evaporation device for high flow rate can be made to correspond to a low flow rate only by changing the control method of the control unit. Can be realized with extremely simple construction.
- the flow rate adjustment valve is controlled based on the measured value of the liquid flow meter that measures the flow rate of the liquefied gas flowing through the liquefied gas sub-pipe. Since the control is based on the measured value of the liquid flow meter with higher accuracy than the gas flow meter, the flow rate can be adjusted with high accuracy.
- the flow rate is low, the liquefied gas flowing through the liquefied gas sub-pipe is decompressed by the decompression means, so that the opening range of the flow rate adjusting valve can be increased compared to when the pressure is not decompressed. As a result, it is possible to control the flow rate adjusting valve in an opening range with good controllability even when the flow rate is high or low.
- FIG. 1 shows an LNG (liquefied natural gas) vaporizer apparatus (hereinafter referred to as “vaporizer apparatus”) 1 according to a first embodiment of the liquefied gas evaporation apparatus of the present invention.
- the vaporizer device 1 is installed in an LNG ship equipped with an LNG storage tank (cargo tank).
- the LNG ship requires a high flow rate natural gas required as a gas replacement gas for the LNG storage tank and a low flow rate natural gas required for fuel such as a boiler or a gas-burning diesel engine.
- the vaporizer device 1 of the present embodiment is capable of supplying a high flow rate gas and a low flow rate gas by evaporating LNG.
- the vaporizer device 1 includes a vaporizer body (evaporator) 3 that evaporates LNG, a main pipe (liquefied gas main pipe) 5 that supplies LNG to the vaporizer body 3, and a vaporizer body 3. And a gas outlet pipe 7 for sending the gas (natural gas) evaporated in the above to the downstream side.
- the vaporizer body 3 is a shell-and-tube heat exchanger, and includes an inlet header 9 that receives the LNG guided from the main pipe 5, a heat exchanger 10 that evaporates the LNG guided from the inlet header 9, and a heat And an outlet header 11 through which gas (natural gas) evaporated by the exchange unit 10 is guided.
- a number of tubes (heat transfer tubes) that circulate LNG are provided inside the heat exchanging unit 10, and the LNG that circulates inside the tubes is outside the tubes by steam supplied from the outside into the heat exchanging unit 10. It is supposed to be heated from.
- the main pipe 5 supplies LNG guided from an LNG storage tank (not shown) to the vaporizer main body 3.
- the pipe diameter of the main pipe 5 is 40A (nominal diameter), for example, and LNG up to about 70 kg / h is circulated.
- the main pipe 5 is provided with a flow rate adjusting valve 6 for adjusting the LNG flow rate supplied to the vaporizer body 3.
- the opening of the flow rate adjusting valve 6 is controlled based on a measured value of a gas flow meter 8 or a liquid flow meter 17 described later.
- a sub pipe (liquefied gas sub pipe) 13 is provided in the main pipe 5 at a position upstream of the flow rate adjusting valve 6 so as to bypass the main pipe 5.
- the pipe diameter of the auxiliary pipe 13 is, for example, 25 A (nominal diameter), and LNG with a flow rate that is a fraction of that of the main pipe 5 is circulated.
- a switching valve 15 is provided between the branch position 5a of the main pipe 5 that branches to the sub pipe 13 and the joining position 5b of the main pipe 5 to which the sub pipe 13 joins. When the switching valve 15 is fully opened, LNG is mainly flowed through the main pipe 5 to obtain a high flow rate, and when the switching valve 15 is fully closed, LNG is caused to flow through the sub pipe 13 to have a low flow rate.
- the operation of the switching valve 15 may be performed by remote control or manually.
- the sub-pipe 13 is provided with a liquid flow meter 17 and a pressure reducing valve (pressure reducing means) 19 in order from the upstream side.
- a pressure reducing valve pressure reducing means
- an orifice may be provided as a fixed pressure reducing means.
- the liquid flow meter 17 for example, a Coriolis flow meter is used, and the liquid flow rate can be directly measured.
- the measured value PV of the liquid flow meter 17 is sent to the liquid flow rate controller 21.
- the liquid flow rate controller 21 transmits an opening degree command OP based on a predetermined function 21a to the flow rate adjustment valve 6 so that the measured flow rate PV obtained by the liquid flow meter 17 becomes a predetermined set value SP. It has become.
- the control of the flow rate adjustment valve 6 by the liquid flow rate controller 21 is performed only when the sub piping 13 is selected by the switching valve 15 and is not performed when the sub piping 13 is not selected by the switching valve 15.
- a temperature adjustment pipe 23 branched from the branch position 5c of the main pipe 5 is provided downstream of the merge position 5b where the sub-pipe 13 joins and upstream of the flow rate adjusting valve 6.
- the pipe diameter of the temperature control pipe 23 is, for example, 40 A (nominal diameter) that is the same diameter as the main pipe 5.
- the downstream end of the temperature adjusting pipe 23 is connected to a slow heatr (temperature regulator) 25 provided on the outlet side of the vaporizer body 3.
- the temperature adjustment valve 27 is controlled by the temperature adjustment controller 31 based on the measured value PV of the temperature sensor 29 provided in the gas outlet pipe 7.
- the temperature adjustment controller 31 transmits an opening degree command OP based on a predetermined function 31 a to the temperature adjustment valve 27 so that the measured temperature PV obtained by the temperature sensor 29 becomes a predetermined set value SP. It has become. Note that the control of the temperature control valve 27 by the temperature control controller 31 is performed both when the sub pipe 13 is selected by the switching valve 15 and when the main pipe 5 is selected by the switching valve 15. .
- a gas vent pipe 33 is branched from a branch point 23 a of the temperature control pipe 23 at a position upstream of the temperature control valve 27. Gas components in the LNG flowing through the main pipe 5 are separated by the gas vent pipe 33.
- the pipe diameter of the gas vent pipe 33 is smaller than the main pipe 5 and the temperature control pipe 23, for example, 25A (nominal diameter).
- the downstream end of the gas vent pipe 33 is connected to the junction 7 a of the gas outlet pipe 7.
- the junction 7 a is provided on the downstream side of the heat sink 25 and on the upstream side of the temperature sensor 29 and the gas flow meter 8.
- the gas vent pipe 33 is provided with a gas vent valve (gas flow rate regulating valve) 35 for adjusting the gas flow rate, and the gas temperature flowing through the gas outlet pipe 7 is adjusted by adjusting the flow rate of the gas vent valve 35. It can be done.
- the gas outlet pipe 7 is connected to the outlet of the vaporizer main body 3, and is provided with a heat sink 25, a junction 7 a, a temperature sensor 29, and a gas flow meter 8 in order from the upstream side.
- the pipe diameter of the gas outlet pipe 7 is, for example, 400 A (nominal diameter), and gas (natural gas) up to about 70 kg / h is circulated.
- gas natural gas
- an orifice flow meter is used as the gas flow meter 8, and the volume flow rate of the gas is measured.
- the control unit (not shown) converts the gas volume flow rate obtained by the gas flow meter 8 into a mass flow rate, and then controls the opening degree of the flow rate adjustment valve 6 so as to become a predetermined set value.
- the control of the flow rate adjusting valve 6 based on the measurement value of the gas flow meter 8 is performed only when the main pipe 5 is selected by the switching valve 15 and is performed when the main pipe 5 is not selected by the switching valve 15. Absent.
- gas flowmeters 8 can be used. For example, a venturi flowmeter may be used instead of the orifice flowmeter.
- the vaporizer device 1 having the above configuration is used as follows. ⁇ For high flow rates> When evaporating LNG having a high flow rate as in the case of gas replacement in the LNG storage tank, the switching valve 15 is fully opened and the main pipe 5 is selected. The flow rate adjustment valve 6 is controlled based on the gas flow meter 8. The LNG guided from the LNG storage tank passes through the operation valve 37, flows through the main pipe 5, and is fully opened without flowing to the sub-pipe 13 to which the flow path resistance is attached by the pressure reducing valve 19. Pass through 15. The LNG that has passed through the switching valve 15 is adjusted to a predetermined flow rate by the flow rate adjusting valve 6 and then flows into the vaporizer body 3.
- the flow rate adjusting valve 6 is controlled by an unillustrated control unit based on the measured value of the gas flow meter 8 so as to satisfy the gas flow rate (set value) required when gas replacement in the LNG storage tank is performed. Done.
- the opening range used by the flow rate adjusting valve 6 at this time is an opening range with good controllability (for example, 70 to 80%). That is, the flow rate adjusting valve 6 is selected according to the conditions at the time of high flow rate.
- the LNG that has flowed into the vaporizer body 3 first flows into the inlet header 9, is then distributed to a large number of heat transfer tubes (not shown), and is heated and evaporated by steam supplied from the outside in the heat exchange unit 10. To do.
- the gas (natural gas) evaporated in the heat exchange unit 10 is brought into an overheated state, led to the outlet header 11, and flowed to the slow heatr 25.
- LNG branched from the branch position 5c of the main pipe 5 and guided through the temperature control pipe 23 is sprayed, and the superheated gas is cooled to a desired temperature.
- the amount of LNG sprayed at this time is adjusted by the temperature control valve 27.
- the temperature adjustment valve 27 is controlled by a temperature adjustment controller 31 based on a measured value of a temperature sensor 29 provided in the gas outlet pipe 7 so as to reach a predetermined target temperature.
- the gas (natural gas) cooled to a predetermined temperature by the slow heat generator 25 is guided to the junction 7 a through the gas outlet pipe 7.
- the gas whose flow rate is adjusted by the gas vent valve 35 is joined via the gas vent pipe 33 branched from the branch position 23a of the temperature control pipe 23.
- the temperature of the gas guided through the gas outlet pipe 5 is finally adjusted by the gas guided from the gas vent valve 33.
- the gas guided from the gas outlet pipe 5 is supplied to the gas phase of the LNG storage tank via a predetermined pipe path (not shown).
- the LNG is depressurized to, for example, 100 kPa or less by the pressure reducing valve 19, and flows into the main pipe 5 at the merging position 5a.
- the LNG reduced in pressure by the pressure reducing valve 19 is adjusted to a predetermined flow rate by the flow rate adjusting valve 6 and then flows into the vaporizer main body 3.
- the flow rate adjusting valve 6 is controlled by the liquid flow rate controller 21 based on the measured value of the liquid flow meter 17 so as to satisfy the gas flow rate (set value) required by the boiler or the gas-burning diesel engine.
- an opening range with good controllability (for example, 70 to 80%) is used as in the case of a high flow rate. That is, even when the flow rate adjusting valve 6 is selected according to the conditions at the time of a high flow rate, the upstream pressure (primary pressure) is reduced, so that an opening range with good controllability can be obtained even at a low flow rate. It has come to be used. Since the operation after the LNG is introduced into the vaporizer body 3 is the same as that at the time of high flow rate, the description thereof is omitted. The gas (natural gas) thus obtained is guided from the gas outlet pipe 5 to a boiler or a gas-burning diesel engine through a predetermined pipe path (not shown).
- the flow rate adjustment valve 6 is controlled based on the measured value of the gas flow meter 8 provided in the gas outlet pipe 7 on the downstream side of the vaporizer body 3.
- the gas flow meter 8 having good measurement accuracy in the flow range set to a high flow rate and the flow rate adjusting valve 6 capable of adjusting the flow rate in the valve opening range having good controllability in the flow rate range are used.
- the gas with a desired flow rate can be supplied with high accuracy.
- the flow rate adjustment valve 6 is controlled based on the measured value of the liquid flow meter 17 that measures the flow rate of the LNG flowing through the auxiliary pipe 13. To do. That is, in the case of a low flow rate, the measurement value of the gas flow meter 8 having an appropriate accuracy in the flow rate range at the time of a high flow rate is not used. This is because the gas flowmeter 8 is used when a high flow rate flows, and thus the measurement accuracy at a low flow rate cannot be guaranteed. Therefore, in the present embodiment, the flow rate of LNG flowing through the sub-pipe 13 is accurately measured by the liquid flow meter 17.
- the temperature control valve 27 since the LNG decompressed by the pressure reduction 27 is introduced when the flow rate is low, it can be opened with high controllability regardless of whether the flow rate is high or low.
- the temperature control valve 27 can be controlled within the temperature range.
- FIGS. 2 a second embodiment of the present invention will be described with reference to FIGS.
- This embodiment is different in that a gas-liquid separator 40 is provided in addition to the first embodiment.
- Other common configurations are denoted by the same reference numerals, and description thereof is omitted.
- the downstream side of the junction 5b where the auxiliary pipe 13 joins the main pipe 5 and the upstream side of the flow regulating valve 6 and the temperature control valve 27 (that is, the upstream side of the branching point 5c). Is provided with a gas-liquid separator 40.
- FIG. 2 the downstream side of the junction 5b where the auxiliary pipe 13 joins the main pipe 5 and the upstream side of the flow regulating valve 6 and the temperature control valve 27 (that is, the upstream side of the branching point 5c).
- the gas-liquid separator 40 includes a container 42 that temporarily stores LNG, and a sealing ball 44 that is provided in the container 42 and has buoyancy with respect to LNG. While the LNG is temporarily stored in the container 42 of the gas-liquid separator 40, the gas components in the LNG in a gas-liquid two-phase flow are separated. The sealing ball 44 floats on the liquid level of the LNG, and the liquid level rises to block the outlet opening 46 having an area smaller than that of the sealing ball 44, thereby suppressing an increase in the liquid level.
- a gas vent pipe 48 is connected to the upper part of the gas-liquid separator 40. Similar to the gas vent pipe 33 shown in FIG. 1, the gas vent pipe 48 includes a gas vent valve 35 and is connected to the gas outlet pipe 7 at the junction 7a.
- the gas-liquid separator 40 having the above configuration is used as follows.
- the LNG is depressurized by the pressure reducing valve 19.
- the LNG may flash to form a gas-liquid two-phase flow.
- LNG made into the gas-liquid two-phase flow flows into the gas-liquid separator 40.
- the gas component is separated.
- the separated gas component (natural gas) is guided to the gas outlet pipe 7 through the gas vent pipe 48 connected to the upper part of the container 42.
- the flow rate is adjusted by the gas vent valve 35 and the temperature of the gas flowing through the gas outlet pipe 7 is adjusted as in the first embodiment.
- the sealing ball 44 rises together with the liquid level and closes the outlet opening 46. Thereby, it is possible to prevent LNG from flowing into the gas vent pipe 48.
- the gas component is separated from the gas-liquid separator 40. Can be removed. Therefore, it can be avoided that LNG that has become a gas-liquid two-phase flow flows into the flow rate adjustment valve 6 and the temperature control valve 27 and obstructs the flow of the liquid phase in the flow rate adjustment valve 6 and the temperature control valve 27.
- the gas-liquid separator 40 ′ shown in FIG. 4 may be used. Specifically, a liquid level sensor 50 that detects the liquid level position may be provided, and the liquid level control valve 52 may be controlled based on the detection value of the liquid level sensor 50. With such a configuration, the sealing ball 44 shown in FIGS. 2 and 3 can be omitted.
- the positional relationship between the liquid flow meter 17 and the pressure reducing valve 19 provided in the sub-pipe 13 is opposite to that in the first embodiment shown in FIG. Such a positional relationship may be adopted.
- LNG has been described as an example of the liquefied gas.
- the present invention is not limited to this, and other liquefied gas may be used, for example, LPG (liquefied propane gas).
- LPG liquefied propane gas
- each embodiment mentioned above demonstrated as a vaporizer apparatus provided in the LNG ship it is not limited to an LNG ship as a ship, It is a ship provided with the tank which stores liquefied gas, such as an LPG ship. Even if it exists, it is applicable.
- the vaporizer device of the present invention can be used for a new ship.
- a low flow rate gas is supplied to a high flow rate vaporizer device installed in an existing ship for fuel gas supply or the like. This is effective when a supply system is additionally installed.
Landscapes
- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- Physics & Mathematics (AREA)
- General Physics & Mathematics (AREA)
- Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Ocean & Marine Engineering (AREA)
- Fluid Mechanics (AREA)
- Automation & Control Theory (AREA)
- General Engineering & Computer Science (AREA)
- Filling Or Discharging Of Gas Storage Vessels (AREA)
Abstract
Description
大型と小型のLNGベーパライザをそれぞれ1台ずつ装備するのは、設置スペースが大きくなり初期投資が嵩むので、大型LNGベーパライザで小型LNGベーパライザを兼用することが好ましい。
LNGベーパライザは、一般に、蒸気加熱式のシェルアンドチューブ式熱交換器を採用しており、チューブ側にLNGを通し、シェル側は飽和蒸気雰囲気とされている。加熱されたLNGは、過熱ガス状態で熱交換器を出て、この過熱ガス状態のガスに対して、熱交換器入口のLNGの一部をバイパスさせて噴霧することで出口温度を調整している。
また、蒸発ガス量は、出口配管に設置したオリフィス流量計またはベンチュリー流量計で容積流量を計測し、質量流量に変換後、質量流量による設定値にあわせて制御する。熱交換器入口側のLNGラインには流量調整弁が設けられ、温調用バイパス流路のLNGラインには温度調整弁が設けられている。これら流量調整弁および温度調整弁は、定格流量にあわせて設計されサイズが決定されるので、極めて少量のLNGを通過させる場合には、十分なLNG流量調整機能やガス温度調整機能が発揮できなくなる。また、低流量では流量計によるガス流量の検知も不正確となり、蒸発量の管理が大変難しい。
しかし、緩熱器105の出口側の流量計109によって流量計測するので、低流量における流量計測精度の改善の余地が依然として残る。
すなわち、本発明の第1の態様にかかる船舶は、液化ガスを導く液化ガス主配管と、該液化ガス主配管から導かれた液化ガスを蒸発させる蒸発器と、該蒸発器にて気化されたガスを導くガス出口配管と、該ガス出口配管に設けられたガス流量計と、前記液化ガス主配管に設けられ、前記蒸発器へ導く液化ガス流量を調整する流量調整弁と、該流量調整弁を制御する制御部と、前記液化ガス主配管から分岐してバイパスし、該液化ガス主配管に再合流するように設けられ、該液化ガス主配管よりも低流量とされた液化ガスが流れる液化ガス副配管と、前記液化ガス主配管と前記液化ガス副配管とを切り換える切換弁と、前記液化ガス副配管を流れる液化ガスの流量を計測する液流量計と、前記液化ガス副配管を流れる液化ガスを減圧する減圧手段とを有する液化ガス蒸発装置を備え、前記制御部は、前記切換弁によって前記液化ガス主配管が選択された場合には、前記ガス流量計の計測値に基づいて前記流量調整弁を制御し、かつ、前記切換弁によって前記液化ガス副配管が選択された場合には、前記液流量計の計測値に基づいて前記流量制御弁を制御し、前記液化ガス蒸発装置から液化燃料ガスが供給される主機を備えている。
一方、液化ガス副配管が選択されて低流量の液化ガスが流れる場合は、液化ガス副配管を流れる液化ガスの流量を計測する液流量計の計測値に基づいて、流量調整弁を制御する。すなわち、低流量の場合には、ガス流量計の計測値を用いないこととした。これは、ガス流量計は高流量が流れる際に用いられるので低流量における測定精度を保証することができないからである。そこで、液化ガス副配管を流れる液化ガスの流量を液流量計で精度良く測ることとした。さらに、低流量の場合には、減圧手段によって液化ガス副配管を流れる液化ガスを減圧することとしたので、減圧しない場合に比べて流量調整弁の開度範囲を大きくすることができる。これにより、高流量の場合でも、低流量の場合でも、精度良く流量計測できるとともに、制御性の良い開度範囲にて流量調整弁を制御することができる。
一方、液化ガス副配管が選択されて低流量の液化ガスが流れる場合は、液化ガス副配管を流れる液化ガスの流量を計測する液流量計の計測値に基づいて、流量調整弁を制御する。すなわち、低流量の場合には、ガス流量計の計測値を用いないこととした。これは、ガス流量計は高流量が流れる際に用いられるので低流量における測定精度を保証することができないからである。そこで、液化ガス副配管を流れる液化ガスの流量を液流量計で精度良く測ることとした。さらに、低流量の場合には、減圧手段によって液化ガス副配管を流れる液化ガスを減圧することとしたので、減圧しない場合に比べて流量調整弁の開度範囲を大きくすることができる。これにより、高流量の場合でも、低流量の場合でも、精度良く流量計測できるとともに、制御性の良い開度範囲にて流量調整弁を制御することができる。
また、低流量の場合には、減圧手段によって液化ガス副配管を流れる液化ガスを減圧することとしたので、減圧しない場合に比べて流量調整弁の開度範囲を大きくすることができる。これにより、高流量の場合でも、低流量の場合でも、制御性の良い開度範囲にて流量調整弁を制御することができる。
[第1実施形態]
図1には、本発明である液化ガス蒸発装置の第1実施形態に係るLNG(液化天然ガス)ベーパライザ装置(以下「ベーパライザ装置」という。)1が示されている。ベーパライザ装置1は、LNG貯蔵タンク(カーゴタンク)を備えたLNG船に設置されている。
LNG船では、LNG貯蔵タンクのガス置換用ガスとして要求される高流量の天然ガスと、ボイラやガス炊きディーゼル機関等の燃料用として要求される低流量の天然ガスとが必要とされる。本実施形態のベーパライザ装置1は、LNGを蒸発させることによって、高流量および低流量のガスを供給可能とするものである。
主配管5には、ベーパライザ本体3へ供給するLNG流量を調整する流量調整弁6が設けられている。流量調整弁6は、後述するガス流量計8または液流量計17の計測値に基づいて開度制御される。
流量調整弁6の上流側位置における主配管5には、主配管5をバイパスするように副配管(液化ガス副配管)13が設けられている。副配管13の配管径は例えば25A(呼び径)とされており、主配管5の数分の1の流量のLNGを流通させるようになっている。
副配管13に分岐する主配管5の分岐位置5aと、副配管13が合流する主配管5の合流位置5bとの間には、切換弁15が設けられている。この切換弁15を全開とすることによりLNGを主として主配管5に流して高流量とし、切換弁15を全閉とすることによりLNGを副配管13に流し低流量とする。切換弁15の操作は、遠隔制御で行っても良いし、手動で行っても良い。
ガス流量計8は、例えばオリフィス流量計が用いられ、ガスの容積流量を計測する。図示しない制御部では、ガス流量計8で得られたガス容積流量を、質量流量に変換した後、所定の設定値となるように流量調整弁6の開度を制御する。ガス流量計8の計測値に基づく流量調整弁6の制御は、切換弁15によって主配管5が選択されているときのみ行われ、切換弁15によって主配管5が選択されていないときは行われない。なお、ガス流量計8としては種々のものが使用可能であり、例えば、オリフィス流量計に代えて、ベンチュリー流量計を用いることとしても良い。
<高流量の場合>
LNG貯蔵タンク内のガス置換を行う場合のように、高流量のLNGを蒸発させる場合には、切換弁15を全開とし、主配管5を選択する。そして、流量調整弁6は、ガス流量計8に基づく制御とする。
LNG貯蔵タンクから導かれたLNGは、操作弁37を通り、主配管5を流れ、減圧弁19にて流路抵抗が付けられている副配管13へは殆ど流れずに全開とされた切換弁15を通過する。切換弁15を通過したLNGは、流量調整弁6にて所定流量に調整された後に、ベーパライザ本体3内へと流れ込む。流量調整弁6は、LNG貯蔵タンクのガス置換を行う際に要求されるガス流量(設定値)を満たすように、ガス流量計8の計測値に基づいて、図示しない制御部によって開度制御が行われる。このときの流量調整弁6で用いられる開度範囲は、制御性の良い開度範囲(例えば70~80%)が用いられる。すなわち、高流量時の条件に合わせて流量調整弁6が選定されている。
緩熱器25では、主配管5の分岐位置5cから分岐されて温調用配管23を介して導かれたLNGが噴霧され、過熱ガスが所望温度まで冷却される。この際に噴霧するLNG量は、温調弁27によって調整される。温調弁27は、ガス出口配管7に設けた温度センサ29の計測値に基づき、所定の目標温度となるよう温調用コントローラ31により制御される。
その後、ガス出口配管5から導かれたガスは、図示しない所定の配管経路を介して、LNG貯蔵タンクのガス相へと供給される。
ボイラやガス炊きディーゼル機関に燃料ガスを供給する場合のように、低流量のLNGを蒸発させる場合には、切換弁15を全閉とし、副配管13を選択する。そして、流量調整弁6は、液流量計17に基づく制御とする。
LNG貯蔵タンクから導かれたLNGは、操作弁37を通り、主配管5を流れ、切換弁15が全閉とされた主配管5へは流れずに、分岐位置5aにて主配管5から分岐された副配管13へと流れ込む。LNGは、副配管13では、液流量計17にて液体流量が計測された後に、減圧弁19にて例えば100kPa以下まで減圧されて、合流位置5aにて主配管5へと流れ込む。減圧弁19にて減圧されたLNGは、流量調整弁6にて所定流量に調整された後に、ベーパライザ本体3内へと流れ込む。流量調整弁6は、ボイラやガス炊きディーゼル機関が要求するガス流量(設定値)を満たすように、液流量計17の計測値に基づいて、液流量コントローラ21によって開度制御が行われる。このときの流量調整弁6で用いられる開度範囲は、減圧弁19にて減圧されているため、高流量時と同様に制御性の良い開度範囲(例えば70~80%)が用いられる。すなわち、高流量時の条件に合わせて流量調整弁6が選定されている場合であっても、上流圧(1次圧)が減圧されているため、低流量でも制御性の良い開度範囲が用いられるようになっている。
ベーパライザ本体3内にLNGが導かれた後の動作は高流量時と同様なので、その説明を省略する。
このようにして得られたガス(天然ガス)は、ガス出口配管5から、図示しない所定の配管経路を介して、ボイラやガス炊きディーゼルエンジンへと導かれる。
主配管5が選択されて高流量のLNGが流れる場合は、ベーパライザ本体3の下流側のガス出口配管7に設けられたガス流量計8の計測値に基づいて、流量調整弁6を制御する。このように、高流量とされた流量範囲にて良い測定精度を有するガス流量計8と、この流量範囲にて制御性の良い弁開度範囲にて流量調整できる流量調整弁6とを用いるので、所望流量のガスを精度良く供給することができる。
一方、切換弁15により副配管13が選択されて低流量のLNGが流れる場合は、副配管13を流れるLNGの流量を計測する液流量計17の計測値に基づいて、流量調整弁6を制御する。すなわち、低流量の場合には、高流量時の流量範囲に適正な精度を有するガス流量計8の計測値を用いないこととした。これは、ガス流量計8は高流量が流れる際に用いられるので低流量における測定精度を保証することができないからである。そこで、本実施形態では、副配管13を流れるLNGの流量を液流量計17で精度良く測ることとした。さらに、低流量の場合には、減圧弁19によって副配管13を流れるLNGを減圧することとしたので、減圧しない場合に比べて流量調整弁6の開度範囲を大きくすることができる。これにより、高流量の場合でも、低流量の場合でも、精度良く流量計測できるとともに、制御性の良い開度範囲にて流量調整弁6を制御することができる。
次に、本発明の第2実施形態について、図2乃至図4を用いて説明する。
本実施形態は、第1実施形態に加えて、気液分離器40を備えている点で相違する。その他の共通する構成については同一符号を付し、その説明を省略する。
図2に示されているように、副配管13が主配管5に合流する合流点5bの下流側でかつ、流量調整弁6及び温調弁27の上流側(すなわち分岐点5cの上流側)には、気液分離器40が設けられている。
気液分離器40は、図3に示すように、LNGを一時的に貯留する容器42と、容器内42内に設けられてLNGに対して浮力を有する封止玉44とを備えている。気液分離器40の容器42内に一時的にLNGが貯留されている間に、気液二相流とされたLNG中のガス成分が分離されるようになっている。封止玉44は、LNGの液面に浮かび、液面が上昇して封止玉44よりも小さい面積を有する出口開口46を閉塞することにより、液面の上昇を抑えるようになっている。気液分離器40の上部には、ガス抜き配管48が接続されている。このガス抜き配管48は、図1に示したガス抜き配管33と同様に、ガス抜き弁35を備えるとともに、合流部7aにてガス出口配管7に接続するようになっている。
低流量時に副配管13が選択されると、LNGは減圧弁19によって減圧される。この際にLNGがフラッシュして気液二相流となる場合がある。このように気液二相流とされたLNGは、気液分離器40へと流れ込む。LNGは、気液分離器40の容器42内で一時貯留されている間に、ガス成分が分離される。分離されたガス成分(天然ガス)は、容器42の上部に接続されたガス抜き配管48を介してガス出口配管7へと導かれる。この際に、ガス抜き弁35によって流量調整を行い、ガス出口配管7を流れるガスの温度を調整する点は、第1実施形態と同様である。
容器42内の液面が上昇すると、封止玉44が液面とともに上昇し、出口開口46を閉塞する。これにより、LNGがガス抜き配管48へと流れ込むことを防止することができる。
また、本実施形態では、図2に示したように、副配管13に設けた液流量計17と減圧弁19との位置関係が図1に示した第1実施形態と逆になっているが、このような位置関係としても良い。
また、本実施形態の気液分離器40,40’を第1実施形態に適用しても良い。具体的には、図1に示した分岐位置23aに気液分離器40,40’を設ける。
また、上述した各実施形態では、LNG船に設けられたベーパライザ装置として説明したが、船舶としてはLNG船に限定されるものではなく、LPG船等の液化ガスを貯蔵するタンクを備えた船舶であっても適用可能である。
3 ベーパライザ本体(蒸発器)
5 主配管(液化ガス主配管)
6 流量調整弁
7 ガス出口配管
7a 合流部
8 ガス流量計
9 入口ヘッダ
10 熱交換部
11 出口ヘッダ
13 副配管(液化ガス副配管)
15 切換弁
17 液流量計
19 減圧弁(減圧手段)
21 液流量コントローラ
21a 関数
23 温調用配管
25 緩熱器(温度調整器)
27 温調弁
29 温度センサ
31 温調用コントローラ
31a 関数
33 ガス抜き配管
35 ガス抜き弁(ガス流量調整弁)
37 操作弁
40,40’ 気液分離器
42 容器
44 封止玉
46 出口開口
48 ガス抜き配管
50 液位センサ
52 液位制御弁
Claims (7)
- 液化ガスを導く液化ガス主配管と、
該液化ガス主配管から導かれた液化ガスを蒸発させる蒸発器と、
該蒸発器にて気化されたガスを導くガス出口配管と、
該ガス出口配管に設けられたガス流量計と、
前記液化ガス主配管に設けられ、前記蒸発器へ導く液化ガス流量を調整する流量調整弁と、
該流量調整弁を制御する制御部と、
前記液化ガス主配管から分岐してバイパスし、該液化ガス主配管に再合流するように設けられ、該液化ガス主配管よりも低流量とされた液化ガスが流れる液化ガス副配管と、
前記液化ガス主配管と前記液化ガス副配管とを切り換える切換弁と、
前記液化ガス副配管を流れる液化ガスの流量を計測する液流量計と、
前記液化ガス副配管を流れる液化ガスを減圧する減圧手段と、
を有する液化ガス蒸発装置を備え、
前記制御部は、前記切換弁によって前記液化ガス主配管が選択された場合には、前記ガス流量計の計測値に基づいて前記流量調整弁を制御し、かつ、前記切換弁によって前記液化ガス副配管が選択された場合には、前記液流量計の計測値に基づいて前記流量調整弁を制御し、
前記液化ガス蒸発装置から液化燃料ガスが供給される主機を備えている船舶。 - 液化ガスを導く液化ガス主配管と、
該液化ガス主配管から導かれた液化ガスを蒸発させる蒸発器と、
該蒸発器にて気化されたガスを導くガス出口配管と、
該ガス出口配管に設けられたガス流量計と、
前記液化ガス主配管に設けられ、前記蒸発器へ導く液化ガス流量を調整する流量調整弁と、
該流量調整弁を制御する制御部と、
前記液化ガス主配管から分岐してバイパスし、該液化ガス主配管に再合流するように設けられ、該液化ガス主配管よりも低流量とされた液化ガスが流れる液化ガス副配管と、
前記液化ガス主配管と前記液化ガス副配管とを切り換える切換弁と、
前記液化ガス副配管を流れる液化ガスの流量を計測する液流量計と、
前記液化ガス副配管を流れる液化ガスを減圧する減圧手段と、
を備え、
前記制御部は、前記切換弁によって前記液化ガス主配管が選択された場合には、前記ガス流量計の計測値に基づいて前記流量調整弁を制御し、かつ、前記切換弁によって前記液化ガス副配管が選択された場合には、前記液流量計の計測値に基づいて前記流量調整弁を制御する液化ガス蒸発装置。 - 前記ガス出口配管に設けられ、液化ガスを散布することによってガス温度を調整する温度調整器と、
前記液化ガス副配管の下流側位置における前記液化ガス主配管から液化ガスの一部を導いて前記温度調整器に液化ガスを散布する温調用配管と、
該温調用配管に設けられた温調弁と、
前記温度調整器から導かれたガスの温度を計測する温度センサと、
を備え、
前記制御部は、前記温度センサの計測値に基づいて、前記温調弁を制御する請求項2に記載の液化ガス蒸発装置。 - 前記液化ガス副配管の下流側位置でかつ前記流量調整弁の上流側位置における前記液化ガス主配管には、気液分離器が設けられている請求項2又は3に記載の液化ガス蒸発装置。
- 前記気液分離器にて分離されたガスを前記ガス出口配管へ導くガス抜き配管と、
該ガス抜き配管に設けられたガス流量調整弁と、
を備え、
前記制御部は、前記温度センサの計測値に基づいて、前記ガス流量調整弁を制御する請求項4に記載の液化ガス蒸発装置。 - 液化ガスを導く液化ガス主配管と、
該液化ガス主配管から導かれた液化ガスを蒸発させる蒸発器と、
該蒸発器にて気化されたガスを導くガス出口配管と、
該ガス出口配管に設けられたガス流量計と、
前記液化ガス主配管に設けられ、前記蒸発器へ導く液化ガス流量を調整する流量調整弁と、
該流量調整弁を制御する制御部と、
前記液化ガス主配管から分岐してバイパスし、該液化ガス主配管に再合流するように設けられ、該液化ガス主配管よりも低流量とされた液化ガスが流れる液化ガス副配管と、
前記液化ガス主配管と前記液化ガス副配管とを切り換える切換弁と、
前記液化ガス副配管を流れる液化ガスの流量を計測する液流量計と、
前記液化ガス副配管を流れる液化ガスを減圧する減圧手段と、
を備えた液化ガス蒸発装置の制御方法であって、
前記制御部により、前記切換弁によって前記液化ガス主配管が選択された場合には、前記ガス流量計の計測値に基づいて前記流量調整弁を制御し、かつ、前記切換弁によって前記液化ガス副配管が選択された場合には、前記液流量計の計測値に基づいて前記流量調整弁を制御する液化ガス蒸発装置の制御方法。 - 液化ガスを導く液化ガス主配管と、
該液化ガス主配管から導かれた液化ガスを蒸発させる蒸発器と、
該蒸発器にて気化されたガスを導くガス出口配管と、
該ガス出口配管に設けられたガス流量計と、
前記液化ガス主配管に設けられ、前記蒸発器へ導く液化ガス流量を調整する流量調整弁と、
該流量調整弁を制御する制御部と、
を備えた液化ガス蒸発装置の改修方法であって、
前記液化ガス主配管から分岐してバイパスし、該液化ガス主配管に再合流するように設けられ、該液化ガス主配管よりも低流量とされた液化ガスが流れる液化ガス副配管と、
前記液化ガス主配管と前記液化ガス副配管とを切り換える切換弁と、
前記液化ガス副配管を流れる液化ガスの流量を計測する液流量計と、
前記液化ガス副配管を流れる液化ガスを減圧する減圧手段と、
を設置するとともに、
前記切換弁によって前記液化ガス主配管が選択された場合には、前記ガス流量計の計測値に基づいて前記流量調整弁を制御し、かつ、前記切換弁によって前記液化ガス副配管が選択された場合には、前記液流量計の計測値に基づいて前記流量調整弁を制御するように前記制御部の制御方法を変更する液化ガス蒸発装置の改修方法。
Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
KR1020147021184A KR101476965B1 (ko) | 2012-03-30 | 2013-03-14 | 선박, 액화가스 증발장치 및 그 제어 방법 및 그 개선 방법 |
CN201380010611.8A CN104136827B (zh) | 2012-03-30 | 2013-03-14 | 船舶、液化气体蒸发装置及其控制方法以及其修改方法 |
EP13769498.0A EP2833046B1 (en) | 2012-03-30 | 2013-03-14 | Vessel, liquefied gas vaporization device, and control method therefor as well as improvement method therefor |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP2012080334A JP2013210045A (ja) | 2012-03-30 | 2012-03-30 | 船舶、液化ガス蒸発装置およびその制御方法ならびにその改修方法 |
JP2012-080334 | 2012-03-30 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2013146316A1 true WO2013146316A1 (ja) | 2013-10-03 |
Family
ID=49259579
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/JP2013/057269 WO2013146316A1 (ja) | 2012-03-30 | 2013-03-14 | 船舶、液化ガス蒸発装置およびその制御方法ならびにその改修方法 |
Country Status (5)
Country | Link |
---|---|
EP (1) | EP2833046B1 (ja) |
JP (1) | JP2013210045A (ja) |
KR (1) | KR101476965B1 (ja) |
CN (1) | CN104136827B (ja) |
WO (1) | WO2013146316A1 (ja) |
Cited By (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2016087023A1 (de) * | 2014-12-06 | 2016-06-09 | Hydac Accessories Gmbh | Verfahren zum ermitteln einer gasmenge nebst vorrichtung zum durchführen dieses verfahrens |
WO2017077718A1 (ja) * | 2015-11-06 | 2017-05-11 | 川崎重工業株式会社 | 船舶 |
JP2017088154A (ja) * | 2015-11-06 | 2017-05-25 | 川崎重工業株式会社 | 船舶 |
CN112303489A (zh) * | 2020-10-26 | 2021-02-02 | 广西电网有限责任公司电力科学研究院 | 一种新型环保绝缘介质的恒温电加热快速充气方法及系统 |
WO2023106290A1 (ja) * | 2021-12-07 | 2023-06-15 | 川崎重工業株式会社 | 液体容器のクールダウン方法及び貯蔵設備 |
Families Citing this family (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP6385134B2 (ja) * | 2014-05-19 | 2018-09-05 | 四国化工機株式会社 | 殺菌剤の送液・霧化装置 |
JP6957165B2 (ja) * | 2017-02-28 | 2021-11-02 | 三菱重工マリンマシナリ株式会社 | ボイラ及びボイラシステム並びにボイラの運転方法 |
JP7009083B2 (ja) * | 2017-05-24 | 2022-01-25 | 株式会社堀場製作所 | 排ガス分析装置及び排ガス分析方法 |
KR102601307B1 (ko) * | 2018-11-14 | 2023-11-13 | 한화오션 주식회사 | 선박용 연료 공급 시스템 및 방법 |
JP7156070B2 (ja) * | 2019-02-12 | 2022-10-19 | Jfeエンジニアリング株式会社 | 燃料ガスの成分調整装置 |
US20210190421A1 (en) * | 2019-12-21 | 2021-06-24 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Method and apparatus for supplying a cryogenic stream with a controlled temperature from a back-up system |
Citations (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH09125077A (ja) * | 1995-11-02 | 1997-05-13 | Kawasaki Heavy Ind Ltd | 液化ガス運搬船用貨物部の熱交換器及びその熱交換装置 |
JP2006177618A (ja) | 2004-12-22 | 2006-07-06 | Mitsubishi Heavy Ind Ltd | 燃料供給装置およびこれを備えたlng船 |
JP2007024198A (ja) * | 2005-07-19 | 2007-02-01 | Chubu Electric Power Co Inc | ボイルオフガスの処理方法及び装置 |
JP2009092163A (ja) * | 2007-10-10 | 2009-04-30 | Chiyoda Corp | 液化天然ガスの受入設備及びその受入方法 |
JP2009204026A (ja) * | 2008-02-26 | 2009-09-10 | Mitsubishi Heavy Ind Ltd | 液化ガス貯蔵設備およびこれを用いた船舶あるいは海洋構造物 |
JP2010025152A (ja) * | 2008-07-15 | 2010-02-04 | Mitsubishi Heavy Ind Ltd | 天然ガス処理設備および液化天然ガス運搬船 |
JP2011105955A (ja) * | 2011-03-03 | 2011-06-02 | Jfe Engineering Corp | 天然ガスの希釈熱量調整方法 |
Family Cites Families (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4341107A (en) * | 1980-10-14 | 1982-07-27 | Tylan Corporation | Calibratable system for measuring fluid flow |
US6672104B2 (en) * | 2002-03-28 | 2004-01-06 | Exxonmobil Upstream Research Company | Reliquefaction of boil-off from liquefied natural gas |
JP4331539B2 (ja) * | 2003-07-31 | 2009-09-16 | 株式会社フジキン | チャンバへのガス供給装置及びこれを用いたチャンバの内圧制御方法 |
JP5148319B2 (ja) * | 2008-02-27 | 2013-02-20 | 三菱重工業株式会社 | 液化ガス再液化装置、これを備えた液化ガス貯蔵設備および液化ガス運搬船、並びに液化ガス再液化方法 |
KR101187532B1 (ko) * | 2009-03-03 | 2012-10-02 | 에스티엑스조선해양 주식회사 | 재액화 기능을 가지는 전기추진 lng 운반선의 증발가스 처리장치 |
US20110023491A1 (en) * | 2009-07-30 | 2011-02-03 | General Electric Company | System and method for supplying fuel to a gas turbine |
-
2012
- 2012-03-30 JP JP2012080334A patent/JP2013210045A/ja active Pending
-
2013
- 2013-03-14 KR KR1020147021184A patent/KR101476965B1/ko active IP Right Grant
- 2013-03-14 CN CN201380010611.8A patent/CN104136827B/zh active Active
- 2013-03-14 EP EP13769498.0A patent/EP2833046B1/en active Active
- 2013-03-14 WO PCT/JP2013/057269 patent/WO2013146316A1/ja active Application Filing
Patent Citations (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH09125077A (ja) * | 1995-11-02 | 1997-05-13 | Kawasaki Heavy Ind Ltd | 液化ガス運搬船用貨物部の熱交換器及びその熱交換装置 |
JP2006177618A (ja) | 2004-12-22 | 2006-07-06 | Mitsubishi Heavy Ind Ltd | 燃料供給装置およびこれを備えたlng船 |
JP2007024198A (ja) * | 2005-07-19 | 2007-02-01 | Chubu Electric Power Co Inc | ボイルオフガスの処理方法及び装置 |
JP2009092163A (ja) * | 2007-10-10 | 2009-04-30 | Chiyoda Corp | 液化天然ガスの受入設備及びその受入方法 |
JP2009204026A (ja) * | 2008-02-26 | 2009-09-10 | Mitsubishi Heavy Ind Ltd | 液化ガス貯蔵設備およびこれを用いた船舶あるいは海洋構造物 |
JP2010025152A (ja) * | 2008-07-15 | 2010-02-04 | Mitsubishi Heavy Ind Ltd | 天然ガス処理設備および液化天然ガス運搬船 |
JP2011105955A (ja) * | 2011-03-03 | 2011-06-02 | Jfe Engineering Corp | 天然ガスの希釈熱量調整方法 |
Non-Patent Citations (1)
Title |
---|
See also references of EP2833046A4 * |
Cited By (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2016087023A1 (de) * | 2014-12-06 | 2016-06-09 | Hydac Accessories Gmbh | Verfahren zum ermitteln einer gasmenge nebst vorrichtung zum durchführen dieses verfahrens |
WO2017077718A1 (ja) * | 2015-11-06 | 2017-05-11 | 川崎重工業株式会社 | 船舶 |
JP2017088154A (ja) * | 2015-11-06 | 2017-05-25 | 川崎重工業株式会社 | 船舶 |
CN112303489A (zh) * | 2020-10-26 | 2021-02-02 | 广西电网有限责任公司电力科学研究院 | 一种新型环保绝缘介质的恒温电加热快速充气方法及系统 |
WO2023106290A1 (ja) * | 2021-12-07 | 2023-06-15 | 川崎重工業株式会社 | 液体容器のクールダウン方法及び貯蔵設備 |
Also Published As
Publication number | Publication date |
---|---|
EP2833046A4 (en) | 2015-10-28 |
KR20140108716A (ko) | 2014-09-12 |
JP2013210045A (ja) | 2013-10-10 |
CN104136827B (zh) | 2016-03-16 |
EP2833046A1 (en) | 2015-02-04 |
KR101476965B1 (ko) | 2014-12-24 |
EP2833046B1 (en) | 2017-03-01 |
CN104136827A (zh) | 2014-11-05 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
WO2013146316A1 (ja) | 船舶、液化ガス蒸発装置およびその制御方法ならびにその改修方法 | |
US10920933B2 (en) | Device and process for refueling containers with pressurized gas | |
US11499765B2 (en) | Device and process for refueling containers with pressurized gas | |
KR20120049731A (ko) | 연료가스 공급장치 및 방법 | |
KR102197740B1 (ko) | 보일러 급수 시스템 및 그것을 구비한 보일러, 보일러 급수 방법 | |
JP2006233796A (ja) | Lng利用発電プラントおよびその運転方法 | |
JP6593024B2 (ja) | ボイラシステム | |
TW200936957A (en) | Method to operate a continuous steam generator and a once-through steam generator | |
JP2011174528A (ja) | 水素ガス充填設備での水素ガス充填方法 | |
KR102050789B1 (ko) | 액화가스의 재기화 장치 및 방법 | |
JP5494819B2 (ja) | Lng気化設備 | |
RU2678156C2 (ru) | Способ и устройство регулирования давления в резервуаре со сжиженным природным газом | |
WO2019230603A1 (ja) | ガス供給ユニット及び混焼発電装置 | |
CN108351072B (zh) | 中间介质式气体气化器 | |
JP2011137608A (ja) | 液化燃料ガス気化装置 | |
KR19980702631A (ko) | 열교환기 장치 | |
WO2011142675A1 (en) | Method for regulating a closed intermediate medium circuit when heat exchanging a primary medium | |
KR101671475B1 (ko) | Lng 재기화 플랜트 | |
JP5473720B2 (ja) | タービン装置及びそのタービン装置を備えた冷熱発電システム | |
JP2013148120A (ja) | 水素ガス充填装置及び水素ガス放散量の測定方法 | |
WO2020226504A1 (en) | A method and a system for heating lng before it enters a storage tank of a ship or other gas | |
WO2023002730A1 (ja) | アンモニア燃料供給設備、及びアンモニア燃料供給方法 | |
WO2019031300A1 (ja) | 液化燃料ガス気化システム、およびそのための温度制御方法 | |
KR101742294B1 (ko) | Lng 재기화 플랜트 및 lng 재기화 방법 | |
DK2625390T3 (en) | Fossil-fired steam generator |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
WWE | Wipo information: entry into national phase |
Ref document number: 201380010611.8 Country of ref document: CN |
|
121 | Ep: the epo has been informed by wipo that ep was designated in this application |
Ref document number: 13769498 Country of ref document: EP Kind code of ref document: A1 |
|
REEP | Request for entry into the european phase |
Ref document number: 2013769498 Country of ref document: EP |
|
WWE | Wipo information: entry into national phase |
Ref document number: 2013769498 Country of ref document: EP |
|
NENP | Non-entry into the national phase |
Ref country code: DE |
|
NENP | Non-entry into the national phase |
Ref country code: DE |