CN110005947A - A kind of Large LNG and air directly exchange heats the system and method that gasify - Google Patents

A kind of Large LNG and air directly exchange heats the system and method that gasify Download PDF

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Publication number
CN110005947A
CN110005947A CN201910388907.2A CN201910388907A CN110005947A CN 110005947 A CN110005947 A CN 110005947A CN 201910388907 A CN201910388907 A CN 201910388907A CN 110005947 A CN110005947 A CN 110005947A
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China
Prior art keywords
air
lng
heat
heat exchanger
natural gas
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CN201910388907.2A
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Chinese (zh)
Inventor
崔华
杨豫森
陈辉
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Hep Energy And Environment Technology Co Ltd
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Hep Energy And Environment Technology Co Ltd
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Priority to CN201910388907.2A priority Critical patent/CN110005947A/en
Publication of CN110005947A publication Critical patent/CN110005947A/en
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Classifications

    • 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
    • F17C13/00—Details of vessels or of the filling or discharging of vessels
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C9/00—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure
    • F17C9/02—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure with change of state, e.g. vaporisation
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2221/00—Handled fluid, in particular type of fluid
    • F17C2221/03—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
    • F17C2225/00—Handled fluid after transfer, i.e. state of fluid after transfer from the vessel
    • F17C2225/01—Handled fluid after transfer, i.e. state of fluid after transfer from the vessel characterised by the phase
    • F17C2225/0107—Single phase
    • F17C2225/0123—Single phase gaseous, e.g. CNG, GNC
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2227/00—Transfer of fluids, i.e. method or means for transferring the fluid; Heat exchange with the fluid
    • F17C2227/01—Propulsion of the fluid
    • F17C2227/0128—Propulsion of the fluid with pumps or compressors
    • F17C2227/0135—Pumps
    • F17C2227/0142—Pumps with specified pump type, e.g. piston or impulsive type
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2227/00—Transfer of fluids, i.e. method or means for transferring the fluid; Heat exchange with the fluid
    • F17C2227/03—Heat exchange with the fluid
    • F17C2227/0302—Heat exchange with the fluid by heating
    • F17C2227/0309—Heat exchange with the fluid by heating using another fluid
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2227/00—Transfer of fluids, i.e. method or means for transferring the fluid; Heat exchange with the fluid
    • F17C2227/03—Heat exchange with the fluid
    • F17C2227/0367—Localisation of heat exchange
    • F17C2227/0388—Localisation of heat exchange separate
    • F17C2227/039—Localisation of heat exchange separate on the pipes

Landscapes

  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Filling Or Discharging Of Gas Storage Vessels (AREA)
  • Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)

Abstract

Directly exchange heat the system and method that gasify the invention discloses a kind of Large LNG and air, system mainly includes LNG storage device, booster pump, air heat exchanger, gas collecting apparatus, hot-air conveying device, natural gas line, LNG gasification heat exchange unit and intermediate medium gas-liquid cycle heat exchange unit.The present invention directly heats LNG using air heat exchanger, and promote natural gas temperature, reduce heat exchanger cost, reduce the influence to environment, avoids the high cost of original seawater heat exchanger requirement titanium tubing, avoid using the variation of ocean temperature caused by heating of seawater, complete LNG gasification and natural gas heating heating, the high fuel cost and operation and maintenance cost that avoid original combustion heater in cost-effective manner.

Description

A kind of Large LNG and air directly exchange heats the system and method that gasify
Technical field
The present invention relates to LNG gasification technical field of heating, and in particular to a kind of to heat LNG using large-scale air heating tower Realize the system and method for gasification.
Background technique
It is planned according to China's energy Long-and Medium-term Development, natural gas will become a bright spot of our country energy development strategy and green One of color energy pillar.Within following time, China will a large amount of inlet natural gas, wherein most natural gas will be with liquefaction The mode of natural gas (LNG) is transported to China.The LNG of a large amount of imports, while a large amount of cold energy is carry, the gasification of LNG at present Rely primarily on seawater to make heat exchange heating and gasifying.
And the problem of seawater heat exchanger and seawater pipeline maximum is to need particulate metal material, tubing and heat exchanger plate Manufacturing cost is high, general using titanium pipe or plate is contained, to avoid chloride ion in seawater to corrosion of metal.If can look for To a kind of heat-exchange system that can be realized as LNG heating and gasifying without seawater, by the very big entirety for reducing LNG seawater to make heat exchange system Equipment manufacturing cost.
Summary of the invention
In view of the deficiencies of the prior art, the present invention is intended to provide a kind of Large LNG and air directly exchange heat gasification system and The cost of LNG gasification can be effectively reduced in method.
To achieve the goals above, the present invention adopts the following technical scheme:
The present invention provides a kind of Large LNG and air directly exchanges heat gasification system, including LNG storage device, booster pump, sky Gas-heat exchanger, gas collecting apparatus, air transport device, natural gas line；The LNG storage device is connected to institute by booster pump The entrance of air heat exchanger is stated, the entrance of the gas collecting apparatus is connected with the outlet of the air heat exchanger, outlet Then it is connected with the natural gas line；The air transport device is used to deliver the air to the surface of air heat exchanger.
Further, the natural gas line be equipped with air dewetting unit, the import of the air dewetting unit and go out Mouth is connected with natural gas line respectively, and for carrying out pre-cooling dehumidifying to hot-air, the hot-air conveying device will be by sky The hot-air of gas Dehumidifying element pre-cooling dehumidifying is delivered to the surface of brethaid.
Further, multiple air heat exchangers are arranged in the system, and the entrance of each air heat exchanger is respectively communicated with There is liquid phase distribution pipe, each liquid phase distribution pipe is connected to the booster pump.
Further, the air transport device includes blower.
Further, the air heat exchanger and air dewetting unit are all made of light pipe type heat-exchanging tube bundle or fin tube type Heat-exchanging tube bundle.
It is directly exchanged heat the method for gasification system the present invention also provides a kind of using above-mentioned Large LNG and air, specifically:
Liquified natural gas LNG enters air heat exchanger by booster pump extraction pressurization from LNG storage device, with air heat The hot-airs of exchanger surfaces carries out heat exchange, and liquified natural gas is boiled to that be gasified totally into low temperature natural by hot air Gas externally supplies natural gas by natural gas line subsequently into gas collecting apparatus even into superheat state.
Further, air dewetting unit is provided on natural gas line, cryogenic natural gas can flow through air dewetting unit； Extraneous hot-air first passes around air dewetting unit, and the cryogenic natural gas in hot-air and air dewetting unit carries out hot friendship It changes, cryogenic natural gas continues through natural gas line conveying after absorbing the heat in hot-air and externally supplies, in hot-air Cooling surface and the discharge for condensing in air dewetting unit of vapor, the hot-air after pre-cooling are sent by air transport device to sky The outer surface of gas heat-exchange device, the LNG in heat exchange device for air outer surface and heat exchange device for air carry out heat exchange, The heat gasification that LNG in heat exchange device for air absorbs air is cryogenic natural gas, and air after cooling is discharged into atmosphere.
Further, when multiple air heat exchangers are arranged in system, liquified natural gas LNG quilt from LNG storage device Booster pump extraction pressurization is introduced into each liquid phase distribution pipe, and each liquid phase distribution pipe distributes liquified natural gas LNG to each In air heat exchanger, heat exchange is carried out with the air outside air heat exchanger.
It directly exchanges heat the design method of gasification system, includes the following steps: the present invention also provides above-mentioned Large LNG and air
S1, according to the capacity of LNG storage device, the flow of LNG booster pump, and final natural gas is required for temperature Degree calculates heat exchange amount required for the LNG of gasification setting flow, including LNG gasification heat exchange amount according to following formula:
QAlways=QGasification+QHeating=FLNG*qLNG latent heat+FLNG*(TFor-T1)*CP gas(1)；
QAlwaysFor LNG gasification and reach feed air temperature needs gross energy, kJ/h；Q gasification is energy needed for LNG gasification, kJ/ h；Q heating is that gaseous natural gas is warming up to energy needed for feed air temperature, kJ/h；FLNGFor LNG stream amount, kg/h；QLNG latent heat is The gasification latent heat of LNG, kJ/kg；CP gasFor the specific heat capacity of natural gas, kJ/kg DEG C；TForFor externally for the temperature of natural gas, DEG C；T1For Temperature after LNG gasification, DEG C；
S2 obtains air and changes in selected light pipe type according to the type of the heat exchanger tube of selection, inquiry design of heat exchanger handbook The convection transfer rate α on the surface of heat pipe or fin tube type heat exchanger tube0；
S4, inquiry LNG liquid phase are into gas phase gasification, in the light pipe type heat exchanger tube or fin tube type heat exchanger tube of selection Heating, gasification and overheat whole process average heat transfer coefficient αi；
QGasification=K0A0△ tm=KfAf△tm (2)
Wherein 1/K0=1/ α0+1/αi；Kf=BK0；△ tm is logarithmic mean temperature difference (LMTD), by light pipe type heat exchanger tube or fin tube type LNG gasification temperature and the outer air themperature of light pipe type heat exchanger tube or fin tube type heat exchanger tube determine in heat exchanger tube；K0It is changed for light pipe type The coefficient of heat transfer of heat pipe, KfFor the coefficient of heat transfer of fin tube type heat exchanger tube, B is to calculate wing using the light pipe type heat exchanger tube coefficient of heat transfer The correction factor of the finned pipe type heat exchanger tube coefficient of heat transfer passes through fin tube type heat exchanger tube internal-external heat exchanger coefficient and the thermal coefficient of tube wall It is calculated；A0For total internal surface area of light pipe type heat-exchanging tube bundle, AfFor total external surface area of fin tube type heat-exchanging tube bundle；
Formula (2) substitution formula (1) can be obtained by and calculate light pipe type heat-exchanging tube bundle or fin tube type heat-exchanging tube bundle The formula of total external surface area of total internal surface area and fin tube type heat-exchanging tube bundle, is calculated light pipe type heat-exchanging tube bundle or finned tube Every fin heat exchange pipe is assigned to just after total internal surface area of formula heat-exchanging tube bundle and total external surface area of fin tube type heat-exchanging tube bundle The design that can complete heat exchanger calculates；
S5, light pipe type heat-exchanging tube bundle or fin tube type heat-exchanging tube bundle are manufactured according to the design calculation result that step S4 is obtained；
S6, it Large LNG and air is completed directly exchanges heat integral installation, connection and the trial operation of gasification system.
The beneficial effects of the present invention are:
1) directly heat LNG using air heat exchanger, and promote natural gas temperature, reduce heat exchanger at This, reduces the influence to environment.
2) the high cost of original seawater heat exchanger requirement titanium tubing is avoided.
3) it avoids and is changed using ocean temperature caused by heating of seawater.
4) LNG gasification and natural gas heating heating are completed in cost-effective manner；
5) the high fuel cost and operation and maintenance cost of original combustion heater are avoided.
Detailed description of the invention
Fig. 1 is the system structure diagram of the embodiment of the present invention 1；
Fig. 2 is integral type fin heat exchange pipe (horizontal fin) schematic diagram in the embodiment of the present invention 1；
Fig. 3 is integral type fin heat exchange pipe (longitudinal wings) schematic diagram in the embodiment of the present invention 1；
Fig. 4 is the schematic diagram of the air dewetting unit (rectangular fin) in the embodiment of the present invention 1；
Fig. 5 is the schematic diagram of the air dewetting unit (Round fin) in the embodiment of the present invention 1.
Specific embodiment
Below with reference to attached drawing, the invention will be further described, it should be noted that the present embodiment is with this technology side Premised on case, the detailed implementation method and specific operation process are given, but protection scope of the present invention is not limited to this reality Apply example.
Embodiment 1
It directly exchanges heat gasification system the present embodiment provides a kind of Large LNG and air, as shown in Figure 1, including LNG storage dress Set 1, booster pump 2, air heat exchanger 3, gas collecting apparatus 4, hot-air conveying device 5, natural gas line 6；The LNG storage dress 1 entrance that the air heat exchanger 3 is connected to by booster pump 2 is set, the entrance of the gas collecting apparatus 4 and the air heat are handed over The outlet of parallel operation 3 is connected, and outlet is then connected with the natural gas line 6；The hot-air conveying device 5 is used for will be hot Air delivery is to the surface of air heat exchanger 3.
In the present embodiment, the natural gas line 6 be equipped with air dewetting unit 7, the air dewetting unit 7 into Mouth and outlet are connected with natural gas line 6 respectively, for carrying out pre-cooling dehumidifying, the hot-air conveying device 5 to hot-air The surface of brethaid 3 will be delivered to by the hot-air of the pre-cooling dehumidifying of air dewetting unit 7.Air dewetting list is used in advance Member, which dehumidifies to hot-air, can prevent the moisture content in hot-air from freezing influence to air heat exchanger, and be promoted simultaneously The temperature of output natural gas, avoids the high fuel cost and operation and maintenance cost of original combustion heater.
In the present embodiment, the hot-air conveying device 5 includes blower.
In the present embodiment, multiple air heat exchangers 3, the entrance point of each air heat exchanger 3 is arranged in the system It is not communicated with liquid phase distribution pipe 8, each liquid phase distribution pipe 8 is connected to the booster pump 2.
In the present embodiment, the air heat exchanger 3 and air dewetting unit 7 are all made of fin tube type heat-exchanging tube bundle.
Specifically, integral type fin heat exchange pipe can be used in the air heat exchanger 3, wherein integral type fin heat exchange pipe packet Include two kinds of horizontal fin (as shown in Figure 2) and longitudinal wings (as shown in Figure 3), fin material and the tubing disposable machine of same metal material Tool machine-shaping can tolerate the ultralow temperature of LNG liquified natural gas.
The air dewetting unit 7 can be used such as Fig. 4 or fin tube type heat exchanger tube shown in fig. 5, the material of fin and light pipe Material is different, and fin can be at round or rectangle, the relatively high air of temperature suitable for cryogenic gaseous natural gas and air heat-exchange Dehumidifying element.
The working principle of above system is:
Liquified natural gas LNG is extracted out by booster pump from LNG storage device and is pressurized, and is then fed into liquid phase distribution pipe, uniformly Distribution liquified natural gas enters air heat exchanger, carries out heat exchange, liquid natural with the hot-air on air heat exchanger surface Gas is boiled to by hot air and is gasified totally into cryogenic natural gas, even into superheat state, subsequently into gas collecting apparatus, Natural gas is externally supplied by natural gas line.
In the present embodiment, air dewetting unit is provided on natural gas line, cryogenic natural gas can flow through air dewetting Unit.Extraneous hot-air first passes around air dewetting unit, and the cryogenic natural gas in hot-air and air dewetting unit carries out Heat exchange, cryogenic natural gas continue through natural gas line conveying after absorbing the heat in hot-air and externally supply, hot-air In cooling surface and the discharge for condensing in air dewetting unit of vapor, the hot-air after pre-cooling is through overfire air conveying device The LNG to the outer surface of heat exchange device for air, in heat exchange device for air outer surface and heat exchange device for air is sent to carry out Heat exchange, the heat gasification that the LNG in heat exchange device for air absorbs hot-air is cryogenic natural gas, and air after cooling is arranged Enter atmosphere.
In the present embodiment, system is provided with multiple air heat exchangers, and liquified natural gas LNG is from LNG storage device It is introduced into each liquid phase distribution pipe by booster pump extraction pressurization, each liquid phase distribution pipe distributes liquified natural gas LNG to each In a air heat exchanger, heat exchange is carried out with the air outside air heat exchanger.
Embodiment 2
The present embodiment provides a kind of design method of system as described in Example 1, specifically:
S1, according to the capacity of LNG storage device, the flow of LNG booster pump, and final natural gas is required for temperature Degree calculates heat exchange amount required for the LNG of gasification setting flow, including LNG gasification heat exchange amount according to following formula:
QAlways=QGasification+QHeating=FLNG*qLNG latent heat+FLNG*(TFor-T1)*CP gas(1)；
QAlwaysFor LNG gasification and reach feed air temperature needs gross energy, kJ/h；Q gasification is energy needed for LNG gasification, kJ/ h；Q heating is that gaseous natural gas is warming up to energy needed for feed air temperature, kJ/h；FLNGFor LNG stream amount, kg/h；QLNG latent heat is The gasification latent heat of LNG, kJ/kg；CP gasFor the specific heat capacity of natural gas, kJ/kg DEG C；TForFor externally for the temperature of natural gas, DEG C；T1For Temperature after LNG gasification, DEG C；
S2 obtains air and changes in selected light pipe type according to the type of the heat exchanger tube of selection, inquiry design of heat exchanger handbook The convection transfer rate α on the surface of heat pipe or fin tube type heat exchanger tube0；
S4, inquiry LNG liquid phase are into gas phase gasification, in the light pipe type heat exchanger tube or fin tube type heat exchanger tube of selection Heating, gasification and overheat whole process average heat transfer coefficient αi；
QGasification=K0A0△ tm=KfAf△tm (2)
Wherein 1/K0=1/ α0+1/αi；Kf=BK0；△ tm is logarithmic mean temperature difference (LMTD), by light pipe type heat exchanger tube or fin tube type LNG gasification temperature and the outer air themperature of light pipe type heat exchanger tube or fin tube type heat exchanger tube determine in heat exchanger tube；K0It is changed for light pipe type The coefficient of heat transfer of heat pipe, KfFor the coefficient of heat transfer of fin tube type heat exchanger tube, B is to calculate wing using the light pipe type heat exchanger tube coefficient of heat transfer The correction factor of the finned pipe type heat exchanger tube coefficient of heat transfer passes through fin tube type heat exchanger tube internal-external heat exchanger coefficient and the thermal coefficient of tube wall It is calculated；A0For total internal surface area of light pipe type heat-exchanging tube bundle, AfFor total external surface area of fin tube type heat-exchanging tube bundle；
Formula (2) substitution formula (1) can be obtained by and calculate light pipe type heat-exchanging tube bundle or fin tube type heat-exchanging tube bundle The formula of total external surface area of total internal surface area and fin tube type heat-exchanging tube bundle, is calculated light pipe type heat-exchanging tube bundle or finned tube Every fin heat exchange pipe is assigned to just after total internal surface area of formula heat-exchanging tube bundle and total external surface area of fin tube type heat-exchanging tube bundle The design that can complete heat exchanger calculates；
S5, light pipe type heat-exchanging tube bundle or fin tube type heat-exchanging tube bundle are manufactured according to the design calculation result that step S4 is obtained；
S6, it Large LNG and air is completed directly exchanges heat integral installation, connection and the trial operation of gasification system.
For those skilled in the art, it can be provided various corresponding according to above technical solution and design Change and modification, and all these change and modification, should be construed as being included within the scope of protection of the claims of the present invention.

Claims (9)

  1. The gasification system 1. a kind of Large LNG and air directly exchange heat, which is characterized in that including LNG storage device, booster pump, sky Gas-heat exchanger, gas collecting apparatus, air transport device, natural gas line；The LNG storage device is connected to institute by booster pump The entrance of air heat exchanger is stated, the entrance of the gas collecting apparatus is connected with the outlet of the air heat exchanger, outlet Then it is connected with the natural gas line；The air transport device is used to deliver the air to the surface of air heat exchanger.
  2. The gasification system 2. Large LNG according to claim 1 and air directly exchange heat, which is characterized in that the natural gas Pipeline is equipped with air dewetting unit, and the inlet and outlet of the air dewetting unit is connected with natural gas line respectively, uses In carrying out pre-cooling dehumidifying to hot-air, the hot-air conveying device is defeated by the hot-air by the pre-cooling dehumidifying of air dewetting unit It send to the surface of brethaid.
  3. The gasification system 3. Large LNG according to claim 1 and air directly exchange heat, which is characterized in that multiple skies are set Gas-heat exchanger, the entrance of each air heat exchanger have been respectively communicated with liquid phase distribution pipe, and each liquid phase distribution pipe is connected to The booster pump.
  4. The gasification system 4. Large LNG according to claim 1 and air directly exchange heat, which is characterized in that the air is defeated Sending device includes blower.
  5. The gasification system 5. Large LNG according to claim 1 and air directly exchange heat, which is characterized in that the air heat Exchanger and air dewetting unit are all made of light pipe type heat-exchanging tube bundle or fin tube type heat-exchanging tube bundle.
  6. 6. a kind of directly exchanged heat the method for gasification system using claim the 1-5 any Large LNG and air, feature It is, specifically:
    Liquified natural gas LNG enters air heat exchanger by booster pump extraction pressurization from LNG storage device, with air heat exchange The hot-air on device surface carries out heat exchange, and liquified natural gas is boiled to by hot air is gasified totally into cryogenic natural gas, very Natural gas is externally supplied by natural gas line subsequently into gas collecting apparatus to superheat state is entered.
  7. 7. according to the method described in claim 6, it is characterized in that, being provided with air dewetting unit, low temperature on natural gas line Natural gas can flow through air dewetting unit；Extraneous hot-air first passes around air dewetting unit, hot-air and air dewetting list Cryogenic natural gas in member carries out heat exchange, and it is defeated to continue through natural gas line after the heat in cryogenic natural gas absorption hot-air It send and externally supplies, cooling surface and the discharge for condensing in air dewetting unit of the vapor in hot-air, the heat sky after pre-cooling Gas is sent by air transport device to the outer surface of heat exchange device for air, is handed in heat exchange device for air outer surface and air heat LNG in changing device carries out heat exchange, and the heat gasification that the LNG in heat exchange device for air absorbs air is cryogenic natural gas, And air after cooling is discharged into atmosphere.
  8. 8. according to the method described in claim 6, it is characterized in that, when multiple air heat exchangers are arranged, liquified natural gas LNG is introduced into each liquid phase distribution pipe from LNG storage device by booster pump extraction pressurization, and each liquid phase distribution pipe is by liquid Natural gas LNG is distributed into each air heat exchanger, carries out heat exchange with the air outside air heat exchanger.
  9. The design method of gasification system 9. a kind of claim 1-5 any Large LNG and air directly exchange heat, feature It is, includes the following steps:
    S1, according to the capacity of LNG storage device, the flow of LNG booster pump, and the required feed air temperature of final natural gas, press Heat exchange amount required for the LNG of gasification setting flow, including LNG gasification heat exchange amount are calculated according to following formula:
    QAlways=QGasification+QHeating=FLNG*qLNG latent heat+FLNG*(TFor-T1)*CP gas(1)；
    QAlwaysFor LNG gasification and reach feed air temperature needs gross energy, kJ/h；Q gasification is energy needed for LNG gasification, kJ/h；Q Heating is that gaseous natural gas is warming up to energy needed for feed air temperature, kJ/h；FLNGFor LNG stream amount, kg/h；QLNG latent heat is LNG's Gasification latent heat, kJ/kg；CP gasFor the specific heat capacity of natural gas, kJ/kg DEG C；TForFor externally for the temperature of natural gas, DEG C；T1For LNG gas Temperature after change, DEG C；
    S2 inquires design of heat exchanger handbook and obtains air in selected light pipe type heat exchanger tube according to the type of the heat exchanger tube of selection Or the convection transfer rate α on the surface of fin tube type heat exchanger tube0；
    The liter of S4, inquiry LNG liquid phase into gas phase gasification, in the light pipe type heat exchanger tube or fin tube type heat exchanger tube of selection The average heat transfer coefficient α of temperature, gasification and overheat whole processi；
    QGasification=K0A0△ tm=KfAf△tm (2)
    Wherein 1/K0=1/ α0+1/αi；Kf=BK0；△ tm is logarithmic mean temperature difference (LMTD), is exchanged heat by light pipe type heat exchanger tube or fin tube type LNG gasification temperature and the outer air themperature of light pipe type heat exchanger tube or fin tube type heat exchanger tube determine in managing；K0For light pipe type heat exchanger tube The coefficient of heat transfer, KfFor the coefficient of heat transfer of fin tube type heat exchanger tube, B is to calculate finned tube using the light pipe type heat exchanger tube coefficient of heat transfer The correction factor of the formula heat exchanger tube coefficient of heat transfer is calculated by the thermal coefficient of fin tube type heat exchanger tube internal-external heat exchanger coefficient and tube wall It obtains；A0For total internal surface area of light pipe type heat-exchanging tube bundle, AfFor total external surface area of fin tube type heat-exchanging tube bundle；
    Formula (2) substitution formula (1) can be obtained by calculate light pipe type heat-exchanging tube bundle or fin tube type heat-exchanging tube bundle it is total in The formula of total external surface area of surface area and fin tube type heat-exchanging tube bundle, is calculated light pipe type heat-exchanging tube bundle or fin tube type changes Every fin heat exchange pipe is assigned to after total internal surface area of heat pipe bundle and total external surface area of fin tube type heat-exchanging tube bundle The design for completing heat exchanger calculates；
    S5, light pipe type heat-exchanging tube bundle or fin tube type heat-exchanging tube bundle are manufactured according to the design calculation result that step S4 is obtained；
    S6, it Large LNG and air is completed directly exchanges heat integral installation, connection and the trial operation of gasification system.
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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114750925A (en) * 2021-01-08 2022-07-15 三菱重工业株式会社 Cold heat recovery system and ship or floating body with same

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114750925A (en) * 2021-01-08 2022-07-15 三菱重工业株式会社 Cold heat recovery system and ship or floating body with same

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