CN103403437A - Liquefied gas regasificaion device and method for manufacturing regasified gas - Google Patents

Liquefied gas regasificaion device and method for manufacturing regasified gas Download PDF

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Publication number
CN103403437A
CN103403437A CN2012800100155A CN201280010015A CN103403437A CN 103403437 A CN103403437 A CN 103403437A CN 2012800100155 A CN2012800100155 A CN 2012800100155A CN 201280010015 A CN201280010015 A CN 201280010015A CN 103403437 A CN103403437 A CN 103403437A
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preheating
heat exchanger
stream
gas
liquid gas
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CN103403437B (en
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冈胜
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MITSUBISHI Shipbuilding Corporation
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Mitsubishi Heavy Industries Ltd
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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
    • F17C7/00—Methods or apparatus for discharging liquefied, solidified, or compressed gases from pressure vessels, not covered by another subclass
    • F17C7/02—Discharging liquefied gases
    • F17C7/04—Discharging liquefied gases 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
    • F17C2201/00—Vessel construction, in particular geometry, arrangement or size
    • F17C2201/05—Size
    • F17C2201/052—Size large (>1000 m3)
    • 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
    • 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
    • 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
    • F17C2225/035—High pressure, i.e. between 10 and 80 bars
    • 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
    • F17C2225/036—Very high pressure, i.e. above 80 bars
    • 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
    • F17C2227/0316—Water 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
    • F17C2227/0302—Heat exchange with the fluid by heating
    • F17C2227/0309—Heat exchange with the fluid by heating using another fluid
    • F17C2227/0316—Water heating
    • F17C2227/0318—Water heating using seawater
    • 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
    • F17C2265/00—Effects achieved by gas storage or gas handling
    • F17C2265/03—Treating the boil-off
    • F17C2265/032—Treating the boil-off by recovery
    • F17C2265/033—Treating the boil-off by recovery with cooling
    • 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
    • F17C2270/0105—Ships

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Filling Or Discharging Of Gas Storage Vessels (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Ocean & Marine Engineering (AREA)

Abstract

A liquefied gas regasification device which can regasify liquefied gas by a shell-and-tube-type heat exchanger with a simple configuration by preheating the liquefied gas with a simple configuration is provided. The liquefied gas regasification device includes a preheating heat exchanger (3) that preheats LNG flowing through a preheated flow (3a) by gasification gas flowing through a preheating flow (3b), and a first shell-and-tube-type heat exchanger (5) that regasifies the LNG preheated in the preheating heat exchanger (3) by seawater or fresh water, the gas regasified in the first shell-and-tube-type heat exchanger (5) being guided to the preheating flow (3b), the liquefied gas regasification plant further including a second shell-and-tube-type heat exchanger (7) that regasifies the LNG condensed through the preheating flow (3b) by seawater or fresh water.

Description

The gasification installation again of liquid gas reaches gasifying gas manufacture method again
Technical field
The present invention relates to a kind of gasification installation again that the liquid gas such as LNG are gasified again and reach gasifying gas manufacture method again.
Background technique
For the LNG(LNG Liquefied natural gas with storing in storage tank) gasify again and be provided to required part, use gasification installation again., as this gasification installation again, mostly adopt open vaporizer (ORV:Open-Rack-type Vaporizer) mode (for example with reference to following patent documentation 1).In this ORV mode, as thermal source, use seawater,, by seawater being spread to the outer surface of a plurality of heat conductive tubes of tabular arrangement in atmosphere, make the LNG gasification of heat conductive tube inside.But there is following problem: need more seawater, and need to guarantee the heat-conducting area of marine stream, therefore be difficult to miniaturization.So the ORV mode is difficult to be arranged on FSRU(Floating Storage and Regasification Unit/ floating and stores and regasification unit), FPSO(Floating Production Storage and Offloading/ floating storage and offloading device) on the boats and ships such as such marine float, LNG ship.
The prior art document
Patent documentation
Patent documentation 1: Japanese kokai publication hei 9-14586 communique
Summary of the invention
The problem that invention will solve
Relative with it,, as the gasification installation again that buoyancy aid is used, boats and ships arrange the ratio ORV mode miniaturization of use, there is the example that uses following gasification installation again: the STV(shell of pipe type vaporizer that the has used shell-and-tube exchanger shown in Figure 3 100) gasification installation again under mode.
The typical construction of this shell-and-tube exchanger 100 is as shown in the drawing, has: the upstream supervisor 103 that LNG flows into; Heat conductive tube 107, be connected with upstream supervisor 103, is set up in parallel a plurality of; Downstream supervisor 105, the LNG that has passed through heat conductive tube 107 flows into.Each heat conductive tube 107 connects in the hydroecium 109 that is surrounded by cylindrical body (housing).Major character as this heat exchanger is that hydroecium 109 is divided into upstream side hydroecium 109a and downstream side hydroecium 109b in the substantial middle section of length direction.In upstream side hydroecium 109a, import seawater (S.W.) from the upstream side (be left side figure) of LNG stream, from the downstream side discharge seawater (with reference to the dotted line this figure) of upstream side hydroecium 109a.That is, in upstream side hydroecium 109a, seawater stream and LNG stream are parallel flows.On the other hand, in the hydroecium 109b of downstream side, import seawater from the downstream side (be right side figure) of LNG stream, from the upstream side discharge seawater (with reference to the dotted line this figure) of downstream side hydroecium 109b.That is, in the hydroecium 109b of downstream side, seawater stream and LNG stream are relative currents.Therefore,, at the minimum upstream side of LNG temperature, use the seawater of high temperature as parallel flow, thereby can avoid freezing of heat conductive tube outer surface, be relative current in the downstream of LNG stream, thereby guarantee that LNG takes out temperature.
But the shell-and-tube exchanger 100 of this mode is compared with the shell-and-tube exchanger 100 ' that hydroecium shown in Figure 4 is Room 1, complex structure, and cost is higher, and has the shortcoming of difficult design.
Therefore, be the formation of the shell-and-tube exchanger 100 ' of Room 1 as adopting hydroecium shown in Figure 4, there is the method for installing in advance preheating LNG with other.For example, IFV(Intermediate-Fluid-type Vaporizer has been proposed: the intermediary formula vaporizer) scheme of mode.In this is called the method for IFV mode, preheating step is set, it is at the upstream side of shell-and-tube exchanger, via anti-freeze type thermal medium such as propane by a heating source such as seawater and indirectly by anti-freeze type thermal medium preheating LNG indirectly.By this preheating step, make the LNG inlet temperature of shell-and-tube exchanger rise to the difficult temperature of freezing that produces, can adopt hydroecium is the shell-and-tube exchanger of the cheapness of Room 1.But have following shortcoming: the required investment of preheating step is larger,, because using the antifreeze liquid such as propane, processes, safeguards more complicated, and the equipment structure also becomes complicated.
The present invention proposes in view of above situation, and it is a kind of simply to construct the preheating of carrying out liquid gas, and the gasification installation again of the liquid gas that can gasify again by the heat exchanger of simple structure that its purpose is to provide.
Be used for the method for dealing with problems
For addressing the above problem, the gasification installation again of liquid gas of the present invention reaches the gasifying gas manufacture method again and adopts following methods.
That is, the gasification installation again of the liquid gas that the 1st mode of the present invention relates to has: the preheating heat exchanger, carry out preheating by the preheating fluid that flows in the preheating stream to being preheated the liquid gas that flows in stream; And the 1st heat exchanger, to use seawater or clear water to gasify again with the liquid gas of heat exchanger preheating by this preheating, in above-mentioned preheating stream, the gas that importing is gasified by above-mentioned the 1st heat exchanger again, the gasification installation again of above-mentioned liquid gas has the 2nd heat exchanger, and the 2nd heat exchanger will use seawater or clear water to gasify again by the liquid gas of above-mentioned preheating stream and condensation.
, with in heat exchanger, will import to by the gas that the 1st heat exchanger gasifies again the preheating stream in preheating, and the preheating liquid gas.Therefore, use the self heat preheating liquid gas of gasification again, by the same fluid that flows, carry out preheating in continuous path, therefore need not to use other thermal medium such as propane in preheating step, simply the formation of structure preheating step.
And, import the liquid gas of using the heat exchanger preheating by preheating in the 1st heat exchanger, make the liquid gas temperature that flow into the 1st heat exchanger increase, can be reduced in therefore that the thermal medium such as seawater or clear water around heat conductive tube is freezed or the possibility of the deterioration of the heat exchange performance that the ice that produces because of heat exchange surface causes.Therefore, when as the 1st heat exchanger, using shell-and-tube exchanger, can adopt hydroecium is the shell-and-tube exchanger of the simple construction of Room 1.
And, import by preheating the preheating stream of heat exchanger and the liquid gas of condensation in the 2nd heat exchanger.When mobile in the preheating stream by the liquid gas of preheating stream, provide heat to the liquid gas that flows in being preheated stream, temperature descends, but in gasifying gas being preheated in flowing the liquid gas that flows and comparing high temperature is directed to the preheating stream, because of this formation, but implementation plan, make liquid gas mobile, cooling in the preheating stream, condensation, can not be cooled to flow into the liquid gas temperature of preheating with heat exchanger.Therefore, can make the liquid gas temperature that flow into the 2nd heat exchanger increase than liquid gas temperature, thereby the same with above-mentioned the 1st heat exchanger, can be reduced in that the thermal medium such as seawater or clear water around heat conductive tube is freezed or the possibility of the deterioration of the heat exchange performance that the ice that produces because of heat exchange surface causes.Therefore, when as the 1st heat exchanger, using shell-and-tube exchanger, can adopt hydroecium is the shell-and-tube exchanger of the simple construction of Room 1.
In addition, to be called " liquid gas " with the fluid that is preheated stream and the outflow of preheating stream of heat exchanger from preheating, but also not only refer to the fluid that only by liquid phase, is formed, be also included within the two-phase fluid that heat exchanger outlet one side has gasified or had predetermined moisture.
And,, as the 1st heat exchanger and/or the 2nd heat exchanger, preferably use shell-and-tube exchanger, but the present invention is not particularly limited, for example the also heat exchanger of above-mentioned ORV mode.
And,, as the thermal medium that adds of the 1st heat exchanger, the 2nd heat exchanger, while using the heating under the secondary closure circuit such as clear water, also can add antifreeze liquid and further take the countermeasure of freezing of thermal medium.
Further, in the gasification installation again of the liquid gas that above-mentioned the 1st mode relates to, also can be provided for making in above-mentioned preheating the cooling flowing path of boil-off gas precooling or condensation with heat exchanger.
Existence is provided with the situation of the equipment that the boil-off gas for the generations such as storage tank that will store liquid gas liquefies again.In this case, by the cooling flowing path that will make boil-off gas precooling or condensation, be arranged on preheating with on heat exchanger, can cooling boil-off gas, and preheating liquid gas more effectively.
Especially, as described below, preferably will be easy to form the plate type heat exchanger of the multithread of a plurality of independently streams, use with heat exchanger as preheating.
Further, in the gasification installation again of the liquid gas that above-mentioned the 1st mode relates to, above-mentioned preheating is with heat exchanger also plate type heat exchanger.
Be plate type heat exchanger by making the preheating heat exchanger, can realize miniaturization.
As plate type heat exchanger, specifically comprise plate and fin type, spiral, preferably use the material of stainless steel, aluminum alloy system.
And the manufacture method of gasifying gas again that the 2nd mode of the present invention relates to has: preheating step, use the preheating heat exchanger, and carry out preheating by the preheating fluid that flows to being preheated the liquid gas that flows in stream in the preheating stream; And the 1st gasification step again, use the 1st heat exchanger, to use seawater or clear water to gasify again by the liquid gas of above-mentioned preheating step preheating, in above-mentioned preheating stream, the gas that importing is gasified by above-mentioned the 1st heat exchanger again, the above-mentioned manufacture method of gasifying gas again has the 2nd gasification step again, uses the 2nd heat exchanger, will use the thermal medium such as seawater or clear water to gasify by the liquid gas of above-mentioned preheating stream and condensation again.
In preheating step in preheating use heat exchanger, will import to by the gas that the 1st heat exchanger gasifies again the preheating stream, and the preheating liquid gas.Therefore, use the self heat preheating liquid gas of gasification again, by the same fluid that flows, carry out preheating in continuous path, therefore need not to use other thermal medium such as propane in preheating step, simply the formation of structure preheating step.
And, in the 1st heat exchanger the 1st again in gasification step, import the liquid gas of use the heat exchanger preheating by preheating, make the liquid gas temperature that flow into the 1st heat exchanger increase, therefore can be reduced in the heat conductive tube possibility freezed of seawater or clear water on every side.Therefore, when as the 1st heat exchanger, using shell-and-tube exchanger, can adopt hydroecium is the shell-and-tube exchanger of the simple construction of Room 1.
And the 2nd in the 2nd heat exchanger in gasification step, imports by preheating the preheating stream of heat exchanger and the liquid gas of condensation again.When mobile in the preheating stream by the liquid gas of preheating stream, provide heat to the liquid gas that flows in being preheated stream, temperature descends, but in gasifying gas being preheated in flowing the liquid gas that flows and comparing high temperature is directed to the preheating stream,, because of this formation, make liquid gas mobile, cooling in the preheating stream, condensation can not be cooled to flow into the liquid gas temperature of preheating with heat exchanger.Therefore, can make the liquid gas temperature that flow into the 2nd heat exchanger increase than liquid gas temperature, therefore can be reduced in the possibility that seawater around heat conductive tube or clear water freeze.Therefore, when as the 2nd heat exchanger, using shell-and-tube exchanger, can adopt hydroecium is the shell-and-tube exchanger of the simple construction of Room 1.
In addition, to be called " liquid gas " with the fluid that is preheated stream and the outflow of preheating stream of heat exchanger from preheating, but and not only refer to the fluid that only by liquid phase, is formed, be also included within the gasification liquefaction of heat exchanger outlet or have the two-phase fluid of predetermined moisture.
And,, as the 1st heat exchanger and/or the 2nd heat exchanger, preferably use shell-and-tube exchanger, but the present invention is not particularly limited, for example the also heat exchanger of above-mentioned ORV mode.
And,, as the thermal medium that adds of the 1st heat exchanger, the 2nd heat exchanger, during the secondary closure circuit such as use clear water, also can add antifreeze liquid.
The invention effect
Use in heat exchanger in preheating, use self the heat that is gasified again by the 1st heat exchanger to carry out the preheating liquid gas, carry out preheating by the same fluid that flows in continuous path, therefore need not to use other thermal medium such as propylene in preheating step, can simply construct and carry out preheating.
And,, by the preheating liquid gas, can reduce the heat conductive tube possibility of freezing on every side of the 1st heat exchanger, can adopt the heat exchanger of simple structure.
And, can make the liquid gas temperature that flow into the 2nd heat exchanger increase than liquid gas temperature, therefore can reduce the possibility that seawater around heat conductive tube or clear water freeze.Therefore can adopt the heat exchanger of simple structure.
Description of drawings
Fig. 1 means the figure of the gasification installation again of the liquid gas that the 1st mode of execution of the present invention relates to.
Fig. 2 means the figure of the variation of Fig. 1.
Fig. 3 means that hydroecium is the longitudinal sectional view of the shell-and-tube exchanger of Room 2.
Fig. 4 means that hydroecium is the longitudinal sectional view of the shell-and-tube exchanger of Room 1.
Embodiment
The mode of execution that the present invention relates to referring to description of drawings.
(the 1st mode of execution)
The 1st mode of execution of the present invention below is described.
At FSRU(Floating Storage and Regasification Unit), FPSO(Floating Production Storage and Offloading) on the boats and ships such as such marine float, LNG ship, LNG bunkerage (liquid gas bunkerage) is set.Fig. 1 represents gasification installation 1 again, and it is used for the LNG(liquid gas that will derive from the LNG storage tank (liquid gas storage tank) of this LNG bunkerage) gasify again while being provided to required part.
As shown in Figure 1, then gasification installation 1 have: the preheating of preheating LNG is with heat exchanger 3; The 1st shell-and-tube exchanger (the 1st heat exchanger) 5, will use the liquid gas of heat exchanger 3 preheatings to use seawater or clear water to gasify by preheating again; The 2nd shell-and-tube exchanger (the 2nd heat exchanger) 7, will use seawater or clear water to gasify with the liquid gas that heat exchanger 3 imports from preheating again.
Preheating is provided with heat exchanger 3: be preheated stream 3a, import the LNG that sends by shifting pump from the LNG storage tank; Preheating stream 3b, import the gasifying gas that gasifies again by the 1st shell-and-tube exchanger 5.
Preheating is plate type heat exchanger with heat exchanger 3.Particularly, comprise plate and fin type, spiral-plate type, preferably use the material of stainless steel, aluminum alloy system.
LNG by being preheated stream 3a by preheating with heat exchanger 3 for example preheating be-160 ℃～-155 ℃ to-100 ℃～-40 ℃.In addition, the fluid after preheating only is called LNG(refers to liquid gas), but be not the fluid that only by liquid phase, is formed, also comprise the two-phase fluid with predetermined moisture.
Gasifying gas utilization by preheating stream 3b is heated the cooling of the LNG by being preheated stream 3a, for example is cooled to approximately 10 ℃ to-100 ℃～-40 ℃.The temperature of the gasifying gas that flows out from preheating stream 3b can use the design of heat exchanger 3 to set by preheating, but preferably is made as the temperature equal with the LNG from being preheated stream 3a outflow.This is because so, can make the 1st shell-and-tube exchanger 5 and the 2nd shell-and-tube exchanger 7 be identical capacity.
The 1st shell-and-tube exchanger 5 is that hydroecium shown in Figure 4 is the shell-and-tube exchanger of the simple structure of Room 1.In hydroecium, seawater or clear water are imported in the mode that becomes relative current with respect to LNG stream.By the 1st shell-and-tube exchanger 5, the LNG after preheating for example is heated to approximately 10 ℃, and is gasified again.
The gasifying gas that gasifies again by the 1st shell-and-tube exchanger 5 as mentioned above, imports to the preheating stream 3b of preheating with heat exchanger 3.
The 2nd shell-and-tube exchanger 7 is the same with the 1st shell-and-tube exchanger 5, is that hydroecium shown in Figure 4 is the shell-and-tube exchanger of the simple structure of Room 1.In hydroecium, seawater or clear water are imported in the mode that becomes relative current with respect to LNG stream.By the 2nd shell-and-tube exchanger 7, LNG cooling with heat exchanger 3 by preheating and condensation for example is heated to 10 ℃ and gasified again.In addition, will use the cooling fluid of heat exchanger 3 only to be called LNG(by preheating and refer to liquid gas), but be not the fluid that only by liquid phase, is formed, also comprise gas phase or have the two-phase fluid of predetermined moisture.
The gasifying gas that gasifies again by the 2nd shell-and-tube exchanger 7 imports to CNG(Compressed natural gas/ compressed natural gas) manifold, be provided to afterwards and need part.
The following use of above-mentioned gasification installation again 1, thus produce gasifying gas again.
The LNG that sends by shifting pump from the LNG storage tank be directed to preheating with heat exchanger 3 be preheated stream 3a, for example be preheating to-100 ℃～-40 ℃ (preheating step).
LNG after preheating imports to the 1st shell-and-tube exchanger 5, by seawater or clear water, for example is heated to approximately 10 ℃, and gasified (the 1st gasification step) more again.
The gasifying gas of gasification imports to the preheating stream 3b of preheating with heat exchanger 3 again,, by the cooling LNG that flows in being preheated stream 3a, for example is cooled to-100 ℃～-40 ℃.
The LNG that flows out from preheating stream 3b imports to the 2nd shell-and-tube exchanger 7, by seawater or clear water, for example is heated to approximately 10 ℃, gasified (the 2nd gasification step) more again.
The gasifying gas of gasification imports to the CNG manifold again, is provided to and needs part.
Gasification installation again 1 according to present embodiment, can play following action effect.
, with in exchanger 3, will import to by the gas that the 1st shell-and-tube exchanger 5 gasifies again preheating stream 3b in preheating, preheating is flowed in being preheated stream 3a LNG.Therefore, use the self heat preheating LNG of gasification again, by the same fluid that flows, carry out preheating in continuous path, therefore need not to use other thermal medium such as propane in preheating step, simply the formation of structure preheating step.
And, import the LNG that use heat exchanger 3 preheatings by preheating in the 1st shell-and-tube exchanger 5, make the LNG temperature that flow into the 1st shell-and-tube exchanger 5 increase, therefore prevent heat conductive tube freezing of seawater or clear water on every side.Therefore, can adopt hydroecium is the shell-and-tube exchanger of the simple construction of Room 1.
And, import the LNG that uses the condensation after the preheating stream 3b of heat exchanger 3 by preheating in the 2nd shell-and-tube exchanger 7.Its design is: when mobile in preheating stream 3b by the LNG of preheating stream 3b, to the LNG that flows, provide heat in being preheated stream 3a, temperature descends, but can not be cooled to flow into the LNG that be preheated stream 3a of preheating with heat exchanger 3.Therefore, can make the LNG temperature that flow into the 2nd shell-and-tube exchanger 7 increase, thereby seawater or clear water can not freeze around heat conductive tube.Therefore, can adopt hydroecium is the shell-and-tube exchanger of the simple construction of Room 1.Especially, in the present embodiment, make the LNG that flows out and flow into the 1st shell-and-tube exchanger 5 from being preheated stream 3a, with the LNG temperature that flows out from preheating stream 3b and flow into the 2nd shell-and-tube exchanger 7, be identical temperature, therefore can make the 1st shell-and-tube exchanger 5 and the 2nd shell-and-tube exchanger 7 be same capability, deployment tube shell-type exchangers at low cost.
(variation)
Fig. 2 represents the variation of the gasification installation again of present embodiment.
This again gasification installation 1 ' cooling flowing path 3c to boil-off gas (hereinafter referred to as " BOG ") precooling or condensation is set in heat exchanger 3 in preheating.Other formations are identical with Fig. 1, and therefore also the description thereof will be omitted for additional same reference character.
BOG invades inevitably and produces because of the heat from LNG storage tank etc., exists cooling and the situation of liquefaction again.When BOG is liquefied again, then liquefaction device is arranged near gasification installation 1 ' again.In this case, the cooling flowing path 3c of precooling or condensation BOG is arranged on preheating with in heat exchanger 3.BOG by cooling flowing path 3c and precooling or condensation imports to condenser or drainer (Condenser or Condensate tank).
Therefore, cooling BOG in cooling flowing path 3c, and by the BOG LNG that flows in being preheated stream 3a of preheating effectively.
Especially, in the present embodiment, as preheating, with heat exchanger 3, use plate type heat exchanger, be easy to realize forming the multithread of a plurality of independently streams.
In addition, in the above-described embodiment, enumerated LNG as liquid gas and described, but the invention is not restricted to this, such as also LPG(liquefied petroleum gas (LPG)), the LEG(liquefied ethylene) etc. other liquid gas.
And, in the above-described embodiment, use the 1st shell-and-tube exchanger and the 2nd shell-and-tube exchanger to be illustrated, but the invention is not restricted to this, even other heat exchangers also can obtain the effect of preheating, the also heat exchanger of ORV mode for example.
Symbol description
1,1 ' gasification installation again
3 preheating heat exchangers
3a is preheated stream
3b preheating stream
The 3c cooling flowing path
5 the 1st shell-and-tube exchangers (the 1st heat exchanger)
7 the 2nd shell-and-tube exchangers (the 2nd heat exchanger)

Claims (5)

1. the gasification installation again of a liquid gas,
Have: the preheating heat exchanger, carry out preheating by the preheating fluid that flows in the preheating stream to being preheated the liquid gas that flows in stream; And
The 1st heat exchanger, will use seawater or clear water to gasify with the liquid gas of heat exchanger preheating by this preheating again,
In above-mentioned preheating stream, import the gas that gasifies again by above-mentioned the 1st heat exchanger,
The gasification installation again of above-mentioned liquid gas has the 2nd heat exchanger, and the 2nd heat exchanger will use seawater or clear water to gasify again by the liquid gas of above-mentioned preheating stream and condensation.
2. the gasification installation again of liquid gas according to claim 1, above-mentioned the 1st heat exchanger and/or above-mentioned the 2nd heat exchanger are shell-and-tube exchangers.
3. the gasification installation again of liquid gas according to claim 1 and 2, be provided for making the cooling flowing path of boil-off gas precooling or condensation on heat exchanger in above-mentioned preheating.
4. the gasification installation again of the described liquid gas of any one of according to claim 1 to 3, above-mentioned preheating heat exchanger is plate type heat exchanger.
5. gasifying gas manufacture method again has:
Preheating step, use the preheating heat exchanger, by the preheating fluid that flows in the preheating stream, to being preheated the liquid gas that flows in stream, carries out preheating; And
The 1st gasification step again, use the 1st heat exchanger, will use seawater or clear water to gasify by the liquid gas of above-mentioned preheating step preheating again,
In above-mentioned preheating stream, import the gas that gasifies again by above-mentioned the 1st heat exchanger,
The above-mentioned manufacture method of gasifying gas again has the 2nd gasification step again, uses the 2nd heat exchanger, will use seawater or clear water to gasify by the liquid gas of above-mentioned preheating stream and condensation again.
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EP2682666A4 (en) 2018-01-17
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