JP2017032146A - Liquefaction gas manufacturing facility and liquefaction gas manufacturing method - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide an air cooling type liquefaction gas manufacturing facility capable of restricting the reduction in liquefaction gas manufacturing amount depending on an ambient temperature by improving the efficiency of heat exchange by AFC.SOLUTION: A liquefaction gas manufacturing facility for manufacturing liquid gas by liquefying supply gas 100 containing methane as a chief constituent, comprises: a first heat exchanger 101; a first refrigerant compressor 200; a second heat exchanger 102; a second refrigerant compressor 300; a first refrigerant air-cooled heat exchanger 201; a first refrigerant air-cooled condenser 211; a second refrigerant air-cooled heat exchanger 301; and a mist spray device for spraying the mist composed of demineralized water into cooling air supplied to the air-cooled heat exchanger or the air-cooled condenser specified among the first refrigerant air-cooled heat exchanger, the second refrigerant air-cooled heat exchanger, the first refrigerant air-cooled condenser, and the second refrigerant air-cooled condenser for cooling the cooling air so as to increase the liquefaction gas manufacturing amount.SELECTED DRAWING: Figure 2

Description

  The present invention relates to a liquefied gas production facility and a liquefied gas production method.

  A liquefied gas production facility is a facility that purifies and liquefies natural gas LNG (Liquid Natural Gas), LPG (Liquid Petroleum Gas), and SNG (Synthetic Natural Gas) to produce a target liquefied gas. . Examples thereof include LNG manufacturing equipment, LPG manufacturing equipment, and SNG manufacturing equipment.

In the LNG manufacturing facility, a water-cooled or air-cooled condenser is used for the refrigeration cycle. Water-cooled condensers often use seawater to cool the cooling water, but the effect of seawater heated by heat exchange on the environment has become a problem. In recent years, LNG that uses air-cooled condensers has become a problem. Manufacturing facilities are increasing.
The liquefaction process is essential not only for LNG production equipment but also for LPG production equipment and SNG production equipment.

  As shown in FIGS. 1 and 2 of Patent Document 1, the LNG manufacturing facility is provided with a pipe rack in the center of the facility, and a compressor, a heat exchanger that cools natural gas, and natural gas are purified on both sides of the pipe rack. It is usual to arrange a distillation column or the like. In an LNG production facility that employs an air-cooled condenser, a plurality of air fin coolers (hereinafter also referred to as “AFC”) are installed on the top of a pipe rack. AFC sucks air from the lower part by a fan, exchanges heat with a fluid flowing through a tube installed in a pipe rack, and discharges air heated by heat exchange from the upper part.

JP 2005-147568 A

  In an LNG production facility that employs an air-cooled heat exchanger, there is a problem that the amount of LNG produced decreases due to a decrease in the amount of AFC heat exchange and a decrease in the output of the gas turbine due to an increase in the outside air temperature.

  Therefore, the present invention provides an air-cooled liquefied gas production facility and an air-cooled liquefied gas production method capable of increasing the efficiency of heat exchange by AFC and suppressing the decrease in the amount of liquefied gas produced depending on the outside air temperature. Objective.

  According to the present invention, a liquefied gas production facility or the like shown in the following items can be provided.

1. A liquefied gas production facility for producing a liquefied gas by liquefying from a supply gas mainly composed of methane,
A first heat exchanger that cools the supply gas and the second refrigerant by heat exchange with the first refrigerant;
A first refrigerant compressor that cools the supply gas and the second refrigerant in the first heat exchanger and compresses the gasified first refrigerant;
A second heat exchanger for further cooling and liquefying the supply gas cooled by the first heat exchanger by heat exchange with the second refrigerant;
A second refrigerant compressor that cools the supply gas in the second heat exchanger and compresses the gasified second refrigerant;
A first refrigerant air-cooled heat exchanger that cools the first refrigerant gas by cooling the first refrigerant gas discharged from the first refrigerant compressor with air;
A first refrigerant air-cooled condenser that liquefies the first refrigerant by cooling the first refrigerant gas cooled by the first refrigerant air-cooled heat exchanger with air;
A second refrigerant air-cooled heat exchanger that cools the second refrigerant gas by cooling the second refrigerant gas discharged from the second refrigerant compressor with air;
A second refrigerant air-cooled condenser that liquefies the first refrigerant by cooling the second refrigerant gas cooled by the second refrigerant air-cooled heat exchanger with air;
The first refrigerant air-cooled heat exchanger, the second refrigerant air-cooled heat exchanger, the first refrigerant air-cooled condenser, and the second refrigerant air-cooled condenser are identified so as to increase the production amount of the liquefied gas. A liquefied gas production facility comprising a mist spraying device for spraying mist composed of demineralized water onto cooling air supplied to an air-cooled heat exchanger or an air-cooled condenser and cooling the cooling air.

If demineralized water is sprayed on all air-cooled heat exchangers (hereinafter referred to as “heat exchanger” also includes “condenser”) provided in the liquefied gas production facility, the heat exchange amount of the heat exchanger increases, The production volume of the liquefied gas production facility can be maximized. However, it is uneconomical because it requires a huge amount of demineralized water.
Therefore, in order to increase the amount of liquefied gas produced, the heat exchanger that sprays the demineralized water is specified, and the demineralized water is sprayed to reduce the amount of demineralized water used, and the liquefied gas production capacity is efficiently Has improved.

  2. Item 2. The liquefied gas production facility according to item 1, wherein the specified air-cooled heat exchanger or air-cooled condenser includes a first refrigerant air-cooled condenser.

The first heat exchanger cools the supply gas and the second refrigerant by indirect heat exchange with the first refrigerant. That is, since the 2nd refrigerant | coolant which liquefies supply gas is also cooled with the 1st refrigerant | coolant, if the cooling capacity of a 1st refrigerant | coolant falls, the liquefied gas production capacity of a liquefied gas production facility will fall remarkably.
Therefore, in item 2, demineralized water is sprayed on the first refrigerant air-cooled condenser.

If mist is sprayed on all the air-cooled heat exchangers provided in the liquefied gas production facility, the heat exchange amount of the heat exchanger is increased, and the production amount of the liquefied gas production facility can be maximized. However, it is uneconomical because it requires a huge amount of demineralized water.
The first heat exchanger cools the supply gas and the second refrigerant by indirect heat exchange with the first refrigerant. That is, since the 2nd refrigerant | coolant which liquefies supply gas is also cooled with the 1st refrigerant | coolant, if the cooling capacity of a 1st refrigerant | coolant falls, the liquefied gas production capacity of a liquefied gas production facility will fall remarkably.
For this reason, in item 2, mist is sprayed only on the first refrigerant air-cooled condenser to reduce the amount of demineralized water used, and the liquefied gas production capacity is efficiently improved.

3. An acid gas removing device for removing the acid gas in the supply gas with an amine solution;
A demineralized water production apparatus for producing demineralized water to dilute the amine solution,
3. The liquefied gas production apparatus according to item 1 or 2, wherein the demineralized water constituting the mist is supplied from the demineralized water production apparatus.

4). The specified air-cooled heat exchanger or air-cooled condenser includes
By calculating with a three-dimensional hydrodynamic equation, the weather field information of the nearby space where the liquefied gas production apparatus is arranged is calculated, and the influence of hot air recirculation (HAR) is large using the weather field information. Item 4. The liquefied gas production facility according to any one of Items 1 to 3, wherein the air-cooled heat exchanger is included.

  Also, there is a problem that warm air exhausted from one AFC is sucked into another adjacent AFC, and HAR reduces the amount of AFC heat exchange and reduces the amount of LNG produced. Can be avoided.

5). Meteorological information set related to a plurality of times within a predetermined period in a first region including a location where the air utilization device is arranged, from a plurality of weather information including at least temperature data and related to the area and time Select multiple
Using the selected plurality of weather information sets as input data, solving a differential equation of the weather information according to an analysis model for weather simulation is related to a plurality of narrower second regions in the first region. Generate multiple first narrow-area weather information sets,
Of the plurality of generated first narrow area weather information sets, select a second narrow area weather information set for the second area including the location,
Item 5. The item according to any one of Items 1 to 4, wherein the second narrow-area meteorological information is calculated by a three-dimensional hydrodynamic equation, and meteorological field information in a nearby space where the liquefied gas production apparatus is arranged is calculated. Liquefied gas production equipment.

6). A liquefied gas production method for producing a liquefied gas by liquefying from a supply gas mainly composed of methane,
Cooling the supply gas and the second refrigerant by heat exchange with the first refrigerant in the first heat exchanger;
In the first refrigerant compressor, cooling the supply gas and the second refrigerant in the first heat exchanger and compressing the gasified first refrigerant;
In the second heat exchanger, the supply gas cooled by the first heat exchanger is further cooled and liquefied by heat exchange with the second refrigerant;
In the second refrigerant compressor, cooling the supply gas in the second heat exchanger and compressing the gasified second refrigerant;
In the first refrigerant air-cooled heat exchanger, cooling the first refrigerant gas discharged from the first refrigerant compressor with air to cool the first refrigerant gas;
In the first refrigerant air-cooled condenser, cooling the first refrigerant gas cooled by the first refrigerant air-cooled heat exchanger with air to liquefy the first refrigerant;
Cooling the second refrigerant gas discharged from the second refrigerant compressor with air in the second refrigerant air-cooled heat exchanger; and cooling the second refrigerant gas;
A second refrigerant air-cooled condenser, wherein the second refrigerant gas cooled by the second refrigerant air-cooled heat exchanger is cooled by air to liquefy the first refrigerant;
The first refrigerant air-cooled heat exchanger, the second refrigerant air-cooled heat exchanger, the first refrigerant air-cooled condenser, and the second refrigerant air-cooled condenser are identified so as to increase the production amount of the liquefied gas. A method for producing a liquefied gas, comprising: spraying a mist composed of demineralized water on cooling air supplied to an air-cooling heat exchanger or an air-cooling condenser, and cooling the cooling air.

  7). The liquefied gas manufacturing method according to item 6, wherein the specified air-cooled heat exchanger or air-cooled condenser includes a first refrigerant air-cooled condenser.

8). In the acid gas removal device, the step of removing the acid gas in the supply gas with an amine solution;
A demineralized water production apparatus comprising: a step of producing demineralized water to dilute the amine solution;
8. The liquefied gas production method according to item 6 or 7, wherein the demineralized water constituting the mist is supplied from the demineralized water production apparatus.

9. The specified air-cooled heat exchanger or air-cooled condenser includes
By calculating with a three-dimensional hydrodynamic equation, the weather field information of the nearby space where the liquefied gas production apparatus is arranged is calculated, and the influence of hot air recirculation (HAR) is large using the weather field information. The method for producing a liquefied gas according to any one of items 6 to 8, wherein the air-cooled heat exchanger or the air-cooled condenser is included.

10. Meteorological information set related to a plurality of times within a predetermined period in a first region including a location where the air utilization device is arranged, from a plurality of weather information including at least temperature data and related to the area and time Select multiple
Using the selected plurality of weather information sets as input data, solving a differential equation of the weather information according to an analysis model for weather simulation is related to a plurality of narrower second regions in the first region. Generate multiple first narrow-area weather information sets,
Of the plurality of generated first narrow area weather information sets, select a second narrow area weather information set for the second area including the location,
Item 10. The item 6-9, wherein the second narrow-area meteorological information is calculated by a three-dimensional hydrodynamic equation to calculate meteorological field information in a nearby space where the liquefied gas production apparatus is arranged. Liquefied gas production method.

It is the schematic which shows an example of LNG manufacturing equipment. It is the schematic which shows the example of LNG liquefaction equipment. It is a figure which shows an example of a function structure of a weather reproduction apparatus. It is a figure which shows an example of the data table of weather information. It is a figure which shows an example of the hardware constitutions of a weather reproduction apparatus. It is a figure which shows an example of wide area weather information. It is a figure which shows the example which expanded the wide area weather information shown in FIG. It is a figure which shows an example of an example of narrow area weather information. It is a figure which shows an example of weather field information. It is a figure which shows an example of AFC in which HAR has arisen. It is the schematic which shows one Embodiment of LNG liquefaction equipment. It is the schematic which shows one Embodiment of arrangement | positioning of LNG manufacturing equipment. It is the schematic which shows one Embodiment of a desalted water supply apparatus. It is the schematic which shows other embodiment of LNG liquefaction equipment.

1. Liquefied gas manufacturing facility The liquefied gas manufacturing facility of the present invention is a liquefied gas manufacturing facility in which a refrigerant is air-cooled by air cooling with an air-cooled heat exchanger to liquefy the gas. In particular, except as noted in the specification, all of the heat exchangers shown below are air-cooled heat exchangers.

  FIG. 1 is a schematic diagram illustrating an example of an LNG manufacturing facility. The gas supplied from the gas field is provided to the LNG manufacturing facility after the liquid separation step. In the LNG production facility, LNG is produced by obtaining respective steps such as mercury removal, acid gas removal, moisture removal, liquefaction, nitrogen removal and the like.

  In the liquefaction step, natural gas is liquefied by a vapor compression refrigeration cycle that uses heat exchange between the compressor power and the condenser. In the refrigeration cycle, gaseous refrigerant is compressed by a compressor, cooled by a condenser to form a high-pressure liquid, and the pressure is reduced by an expansion valve or the like, and heat is exchanged with natural gas using a low-temperature refrigerant. The refrigerant after the heat exchange becomes a gas and is supplied to the compressor for circulation.

  The acid gas removal is performed by separating the acid gas and the process gas by chemical absorption separation using an amine solvent.

  More specifically, the liquefied gas production facility of the present invention is a liquefied gas production facility having a liquefied gas production section that removes unnecessary substances from a supply gas mainly composed of methane and liquefies to produce a liquefied gas. The liquefied gas production unit includes a heat exchanger that cools the supply gas by exchanging heat with the refrigerant, a compressor that compresses the refrigerant evaporated by heat exchange with the supply gas, and the compressed refrigerant An air fin cooler unit that cools the cooled refrigerant, and an expansion unit that adiabatically expands and cools the cooled refrigerant, and the air fin cooler unit includes a demineralized water supply device that sprays demineralized water.

  According to the liquefied gas production facility of the present invention, the desalted water is sprayed in the form of mist or droplets on the lower portion of the air fin cooler by the desalted water supply device. The sprayed demineralized water is sucked upward by the air fin cooler accompanied by the air sucked from the lower part thereof. The sucked-up demineralized water evaporates while passing between the tubes installed on the pipe rack and being discharged from the upper part of the air fin cooler. The heat of vaporization at this time can efficiently cool the refrigerant flowing through the tubes laid on the pipe rack, and can suppress the decrease in the heat exchange amount depending on the outside air temperature and HAR. As a result, the liquefied gas A decrease in production amount can be suppressed.

  Demineralized water means water from which salts have been removed. Examples thereof include deionized water that has passed through an ion exchange resin, RO water that has passed through a reverse osmosis membrane, and distilled water. By using demineralized water, the scale derived from the salt does not adhere to the tube or the air fin cooler, and a factor that leads to a decrease in the heat transfer coefficient can be eliminated.

FIG. 2 is a schematic diagram illustrating an example of a liquefaction facility among LNG production facilities.
The supply gas 100 from which typical impurities CO ₂ , H ₂ S, and water are removed is sent to the liquefaction facility as a process fluid, and the supply gas is cooled by two refrigerants having different temperatures, and finally, Liquefied. The refrigerant having a high temperature (first refrigerant) is, for example, propane. The second refrigerant having a low temperature is, for example, a mixed refrigerant composed of nitrogen, methane, ethane, and propane.

  In FIG. 2, it is cooled and liquefied by the heat exchanger 101 using the first refrigerant as the refrigerant and the heat exchanger 102 using the second refrigerant as the refrigerant. The LNG product is sent to the storage tank 105 by the pump 104 and stored until shipment. The gas slightly warmed in the storage tank and vaporized from LNG is returned to the process again, liquefied again in the heat exchanger 103, and sent to the storage tank 105 by the pump 104.

  In the first refrigerant cooling cycle, the first refrigerant collected from the intake lines 203, 204, 205 is pressurized by the first refrigerant compressor 200, then cooled by the first refrigerant air-cooled heat exchanger 201, The refrigerant is liquefied by the first refrigerant air-cooled condenser 211, depressurized to a predetermined pressure by the expansion valve 202, and then sent to the heat exchanger 101. In the heat exchanger 101, the supply gas 100 and the second refrigerant used in the subsequent heat exchanger are cooled by heat exchange with the first refrigerant.

  In the second refrigerant cooling cycle, the second refrigerant collected from the intake lines 303 and 304 is pressurized by the second refrigerant compressor 300 and then cooled by the second refrigerant air-cooled heat exchanger 301, and further the heat exchanger. In 101, it is cooled and liquefied by heat exchange with the first refrigerant. Next, the pressure is reduced to a predetermined pressure by the expansion valve 302 and then sent to the heat exchanger 102. In the heat exchanger 102, the supply gas 100 output from the heat exchanger 101 is cooled and liquefied.

  According to the present invention, desalted water is sprayed from the lower portion of the air fin cooler 100A by a desalted water supply device (not shown).

2. The liquefied gas manufacturing method The liquefied gas manufacturing method of the present invention is a liquefied gas manufacturing method in which an unnecessary substance is removed from a supply gas containing methane as a main component and liquefied to produce a liquefied gas. A step of cooling by exchanging heat with the gas, a step of compressing the refrigerant evaporated by heat exchange with the supply gas, a step of cooling the compressed refrigerant by an air fin cooler, and adiabatic expansion of the cooled refrigerant And demineralized water is sprayed from the lower part of the air fin cooler.

  According to the liquefied gas production method of the present invention, by spraying demineralized water from the lower part of the air fin cooler, the sprayed demineralized water is sucked upward by being accompanied by the air sucked from the lower part by the air fin cooler. . The sucked-up demineralized water evaporates while passing between the tubes installed on the pipe rack and being discharged from the upper part of the air fin cooler. The heat of vaporization at this time can efficiently cool the refrigerant flowing through the tubes laid on the pipe rack, and can suppress the decrease in the heat exchange amount depending on the outside air temperature and HAR. As a result, the liquefied gas A decrease in production amount can be suppressed.

  The sprayed demineralized water may be in the form of a mist or a droplet, and the diameter of the droplet is not particularly limited, but the smaller the diameter, the better. The spray amount of the desalted water can be changed as appropriate in consideration of the outside air temperature and the state of occurrence of HAR. Preferably, the spray amount of the desalted water is from the upper part of the air fin cooler until it is discharged. The amount is such that the whole amount evaporates.

  The air fin cooler that sprays the demineralized water is preferably a part of the air fin cooler among the air fin coolers used for producing the liquefied gas. In order to spray demineralized water on all air fin coolers used for liquefied gas production, a large-scale demineralized water supply device is required. Thus, the required amount of desalted water can be suppressed, and the equipment cost and operating cost for the production and spraying of desalted water can be reduced.

  Moreover, it is preferable that the one part air fin cooler which sprays demineralized water is an air fin cooler with a large influence on the amount of liquefied gas production. By spraying demineralized water onto a specific air fin cooler that has a large impact on the amount of liquefied gas produced, the required amount of demineralized water can be suppressed, and the amount of heat exchange depending on the outside air temperature and HAR can be reduced. A decrease in the amount of liquefied gas produced can be suppressed.

3. Identifying an air fin cooler that sprays demineralized water by simulation Air fin coolers that have a large impact on the production volume of liquefied gas are, for example, air fin coolers that have a large heat transfer area (heat exchange amount) and air fin coolers that have a large impact on HAR. Etc. The effect of HAR can be analyzed by simulation.

3.1 Meteorological Analysis Model An example in which the above-described simulation (numerical fluid analysis) is performed by a weather reproduction device using output data of the weather analysis model shown below will be described.

  When measuring the temperature and wind direction in the area where the gas liquefaction plant is located, the design of the gas liquefaction plant needs to be designed taking into account the effects of annual changes such as the presence or absence of El Nino phenomenon. It is necessary to measure the crossing temperature and wind direction. However, when there is no such aged data, it is difficult to newly measure the temperature and the wind direction over a plurality of years, so it was necessary to design a gas liquefaction plant based on environmental data with low accuracy.

  The meteorological analysis model includes various physical models, and by solving them with a computer, weather simulation with high spatial resolution can be performed to perform weather simulation. The advantage of weather simulation is that it can estimate weather information with higher spatial resolution than field observations.

  In order to perform a weather simulation, it is necessary to capture initial value and boundary value data from a weather database downloaded from a network. In order to design an LNG manufacturing facility, there is not enough detailed spatial resolution, but as weather information regarding a wide area including an area where the LNG manufacturing facility is located (hereinafter referred to as “wide area weather information”), for example, NOAA ( There is National Centers for Environmental Prediction (NCEP), which is globally analyzed objectively re-evaluated every 6 hours. NCEP data as regional meteorological information is based on meteorological elements (wind direction, wind speed, turbulent energy, solar radiation, atmospheric pressure, etc.) on a three-dimensional lattice point when the world is divided into a grid (grid spacing is 1.5 to 400 km). Rainfall, humidity, and temperature) are prepared every 6 hours. According to the present embodiment, since it is necessary to design in consideration of the influence of yearly changes such as the presence or absence of El Niño phenomenon, wide-area weather information (for example, the above-mentioned NCEP data) over a plurality of years is converted into initial values and boundary values. Use as data.

  A physical model included in the weather analysis model is, for example, WRF (The Weather Research & Forecasting Model). The WRF includes various physical models. Physical models include radiation models that calculate solar radiation and atmospheric radiation, turbulence models that represent turbulent mixed layers, ground surface temperature, soil temperature, soil moisture content, snow cover, and ground surface flux. There are surface models.

  The meteorological analysis model described partial differential equations representing fluid motion in the atmosphere, including Naviestokes' equations related to fluid motion and empirical equations derived from atmospheric observation results, and conservation laws for mass and energy A weather simulation can be executed by including the partial differential equation and solving the differential equation simultaneously. Therefore, by using the regional weather information as the input data as the initial value and the boundary value, solving the differential equation according to the weather analysis model for the weather simulation, the LNG manufacturing facility related to the area of spatial resolution narrower than the regional weather information The weather information of the arrangement area can be generated. The weather information generated in this way is referred to as “narrow area weather information”.

3.2 Computational fluid analysis Computational fluid analysis is a numerical analysis and simulation method for observing a flow by applying computational fluid dynamics (CFD) by solving a fluid motion equation with a computer. Specifically, the fluid state is calculated spatially by the Finite Volume Method using the Naviestokes equation, which is a fluid dynamic equation. The numerical fluid analysis procedure includes 3D model data creation process that reproduces the structure of the facility to be examined, a grid generation process that divides the examination target range into a grid that is the minimum calculation unit, and a computer. Including a step of taking in values and boundary values, solving a hydrodynamic equation in each lattice, and outputting various values (flow velocity, pressure, etc.) obtained as a result of the analysis as an image such as contour display or vector display.

  Numerical fluid analysis can realize fluid simulation with higher resolution than the weather analysis model, so it is very difficult to reproduce by weather simulation, and small changes in wind speed and direction, and several centimeters to several meters scale It is possible to provide information on the air flow phenomenon peculiar to the spatial scale, such as the change of the air flow around the building from the disturbance of the air flow.

3.3 Functional configuration and hardware configuration of the weather reproduction device The weather reproduction device performs a weather analysis model and a numerical fluid analysis to calculate narrow-area weather information in a narrow area where the LNG manufacturing facility is located. .

  FIG. 3 is a diagram illustrating an example of a functional configuration of the weather reproduction device. The weather reproduction device 90 shown in FIG. 3 includes a storage unit 12 that stores data and programs, and a processing unit 14 that performs numerical calculation processing. The storage unit 12 includes a weather analysis program 901 such as WRF, a numerical fluid analysis program 903, a design temperature calculation program 905, a wind map generation program 907, a drawing output program 909 for generating a layout map, a weather database 800, NCEP data, and the like. Wide area weather information 801, narrow area weather information 803 obtained by weather simulation, airflow field information 805 obtained by numerical fluid analysis, temperature analysis data 807, wind direction analysis data 808, and layout map data 809 are stored. The weather database holds wide-area weather data 801 and is downloaded from outside or obtained through a storage medium.

  The processing unit 14 executes the weather analysis program 901 to generate the narrow area weather information 803 from the wide area weather information 801 and perform the weather analysis process stored in the storage unit 12. Further, the processing unit 14 executes the numerical fluid analysis program 903 to generate the airflow field data 807 from the narrow area weather information 803 and perform numerical fluid processing stored in the storage unit 12.

  Further, the processing unit 14 executes the layout map generation program 909 and outputs layout map data 809 based on the wind direction analysis data 808.

  FIG. 4 is a diagram illustrating an example of a weather information data table. The data table shown in FIG. 4 shows the wide area weather information 801, but is also a data table applied to the narrow area weather information 803. However, the wide-area weather information includes the area targeted for the narrow-area weather information, and covers the broad-area weather information. As shown in FIG. 4, weather information is shown as a record set of a plurality of records composed of various data of wind direction, wind speed, turbulent energy, solar radiation, atmospheric pressure, rainfall, humidity, and temperature with time as a main key. . In other words, it is a weather information set classified by temperature, and the wide area weather information 801 and the narrow area weather information 803 are a plurality of weather information sets classified by area.

  FIG. 5 is a diagram illustrating an example of a hardware configuration of the weather reproduction device. The weather reproduction device 90 shown in FIG. 5 includes a processor 12A, a main storage device 14A, an auxiliary storage device 14B such as a hard disk and an SSD (Solid State Drive), a drive device 15 that reads data from the storage medium 900, and a NIC (network A communication device 19 such as an interface card, and these components are connected to each other by a bus 20. The weather reproduction device 90 is connected to an external display 16 as an output device and an input device 17 such as a keyboard and a mouse. The processing unit 12 illustrated in FIG. 3 corresponds to the processor 12A, and the storage unit 14 corresponds to the main storage device 14A.

  In the storage medium 900, the weather database 800, the weather analysis program 901, the numerical fluid analysis program 903, the design temperature calculation program 905, the wind map generation program 907, and the layout map generation program 909 shown in FIG. 3 are stored as data. May be. These data 800 to 909 are stored in the storage unit 12 as shown in FIG.

  The weather reproduction device 90 may be connected to the external server 200 and the computers 210 and 220 via the network 40. The computer 210 and the external server 200 may have the same components as the weather reproduction device 90. For example, the weather database 800 in the server 200 can be received via the network 40. Further, among the programs shown in FIG. 3, only the weather analysis program 901 related to the weather simulation with a high system load is stored in the weather reproduction device 90, and the other programs are stored in either of the computers 210 and 220. It may be executed.

  In the above description, the computer is limited to hardware, but the weather reproduction device 90 may be a data center virtual server. In that case, the hardware form may be such that the programs 901 to 909 are stored in the storage unit of the data center, are executed by the processing unit of the data center, and data is output from the data center to the client computer. The external server 200 may have a weather database. In that case, the weather reproduction device 90 acquires wide-area weather data from the external server 200.

3.4 Reproduction of weather information in the vicinity of an LNG manufacturing facility FIG. 6 is a diagram showing an example of wide area weather information. FIG. 6 shows wide-area weather information A100 on a map of Japan.

  FIG. 7 is a diagram showing an example in which the wide-area weather information shown in FIG. 6 is enlarged. The wide area weather information A100 illustrated in FIG. 7 indicates an area where the LNG manufacturing facility 100 is disposed. 1100 indicates a coastline. The left side of the Wangan Line 1100 is the sea, and the right side is the land. FIG. 8 is a diagram illustrating an example of narrow-area weather information. FIG. 8 shows a region to be subjected to the weather simulation. The region is divided into a plurality of regions A1 to A15 for performing the weather simulation, and each corresponds to a calculation grid. For example, when the grid resolution is 9 km, the calculation area is 549 km × 549 km, and when the grid resolution is 1 km, the calculation area is 93 km × 93 km. Therefore, in these areas A1 to A15, evaluation points are set in a lattice pattern at a distance interval of 1 to 9 km in the east-west direction and the north-south direction.

  As shown in FIG. 8, the LNG manufacturing facility 100 is arranged, and in order to obtain the temperature or wind direction of the area, the processing unit 12 solves the differential equation of the weather information according to the weather analysis model for the wide area weather information A100. The narrow-area weather information A1 to A16 is generated.

  FIG. 9 is a diagram illustrating an example of weather field information. The processing unit 12 performs numerical fluid analysis on the narrow area weather information A16 shown in FIG. 9 and calculates weather field information in a narrower area than the narrow area weather information. After calculating the area A15, detailed weather field information around the LNG manufacturing facility 100 may be obtained using a hydrodynamic model (CFD model) with the weather field information in the area A15 as an initial value. In this case, it can be obtained in 0.5 m increments much smaller than the grid resolution (for example, 1 km) of the weather simulation.

  Since the weather field information in the target area A16 in which the LNG manufacturing facility 100 is arranged can be obtained using a fluid dynamic model, it is possible to obtain precise data that takes into account the shape of the building. Examples of the hydrodynamic model include K · ε, LES, DNS, and the like.

  Since the calculation apparatus according to the present embodiment needs to obtain detailed data only for the weather field information of the target region, it is not necessary to perform CFD model analysis on all of the region A1 to region A15. Therefore, the accuracy can be improved and the processing time can be shortened by performing the CFD analysis only on the target region without requiring an enormous calculation time by the CFD model analysis.

  Reference numeral 320 in FIG. 9 denotes the exhaust gas recirculation flow. By the CFD analysis, it is possible to calculate and clarify the flow of the warm air exhaled by the LNG manufacturing facility, which has not been clarified by the weather simulation, and recirculates to the suction portion of the LNG manufacturing facility. In addition, the flow of recirculation can be known, whereby the AFC having a large influence of HAR can be determined.

  Further, for example, when there is an airfield in A3 in FIG. 8 and necessary temperature data and observation data of wind direction data are available, a set of the first narrow area weather information is set using those data as input values. It may be recalculated. This can improve the accuracy of weather simulation using available local data.

  Further, the area A16 where the LNG manufacturing facility is arranged may differ from the topography of the weather information depending on any of the leveling, land use, and facility installation. Even in such a case, the first set of narrow-area meteorological information may be recalculated based on the terrain information reflecting any of the leveling, land use, and equipment installation, depending on the arrangement of the LNG manufacturing equipment. This makes it possible to accurately simulate the weather conditions after the LNG manufacturing facility is constructed.

FIG. 10 is a diagram illustrating an example of AFC in which HAR occurs. FIG. 10 shows the high and low temperatures by color shading. The darker the color, the higher the temperature and the greater the influence of HAR.
Among the propane capacitors, an AFC having a particularly large HAR can be identified.

  As described above, for the design of a gas liquefaction plant, AFC, which has a large HAR business, reproduces the weather by weather simulation, generates narrow-area weather information, and performs CFD analysis using these data. Become clear. Therefore, even when there is no aged data, it is possible to design and construct a gas liquefaction plant that has HAR countermeasures.

  In the above example, the CFD analysis is performed from the calculation result of the weather simulation. However, the CFD analysis may be performed without using the calculation result of the weather simulation. In this case, it corresponds to a case where CFD analysis is performed without using a weather simulation based on an actual measurement value or the like, or a case where only CFD analysis is performed with reduced accuracy.

  In an air-cooled LNG production facility, there are many AFCs, and spraying demineralized water on all of them increases the consumption of demineralized water. Therefore, in the 1st refrigerant | coolant air-cooled condenser 211, the consumption of demineralized water can be suppressed by pinpointing AFC with a large influence of HAR by simulation and spraying demineralized water on it.

  Moreover, it is preferable to perform a CFD analysis and to spray demineralized water intermittently when the influence of HAR is large. Thereby, the reduction | decrease of the liquefied gas production amount by the influence of HAR can be suppressed.

  Hereinafter, specific embodiments of the present invention will be described with reference to the accompanying drawings. The scope of the present invention is not limited to the description of these examples.

Example 1
FIG. 11 is a schematic diagram showing an embodiment of a liquefaction facility among LNG manufacturing facilities. This process is also called a mixed refrigerant (hereinafter referred to as “MR”) composed of propane (hereinafter also referred to as “C3”), nitrogen, methane, ethane, and propane as a refrigerant for cooling and liquefying natural gas. ) And is also called a C3-MR system.

  FIG. 11 shows a flow of natural gas (or LNG) as a process fluid (indicated by a thin solid line), a flow of a first refrigeration cycle using propane as a working fluid (indicated by a thick solid line), and a mixed refrigerant. A flow (indicated by a dotted line) of the second refrigeration cycle as a working fluid is shown. The flow of propane and the flow of the mixed refrigerant constitute an independent closed loop circulated by the compressor driving device. A gas turbine and a motor (not shown) for driving the compressor are connected to the propane (C3) compressor 20 and the two mixed refrigerant (MR) compressors 40 and 42 connected in series, respectively.

  The C3 compressor 20 pressurizes propane, which is a refrigerant in the first refrigeration cycle, and is driven by a single-shaft gas turbine (not shown). The low-pressure stage MR compressor 40 and the high-pressure stage MR compressor 42 pressurize a mixed refrigerant composed of a mixture of nitrogen, methane, ethane and propane, which is a refrigerant of the second refrigeration cycle, in two stages. These MR compressors 40 and 42 are simultaneously driven by a gas turbine and a motor (not shown).

  The propane refrigerant pressurized by the C3 compressor 20 circulates in the first refrigeration cycle indicated by a thin solid line, and the mixed refrigerant pressurized by the MR compressors 40 and 42 circulates in the second refrigeration cycle indicated by a dotted line. .

  The purified natural gas 10 from which carbon dioxide and hydrogen sulfide have been removed in advance by an acid gas treatment device is first a high-pressure propane refrigerant (pressure 770 kPa (7.7 bar), temperature 17 ° C.) at a pressure of about 5 MPa (50 bar). In the heat exchanger 11 through which the water flows, it is cooled to about 21 ° C., and most of the water is condensed and then separated by the drum 12. The natural gas thus dehydrated is cooled to −10 ° C. in the heat exchanger 13 through which a medium-pressure propane refrigerant (pressure 320 kPa (3.2 bar), temperature −13 ° C.) flows, and then further reduced pressure propane. It is cooled to −30 ° C. in the heat exchanger 14 through which the refrigerant (pressure 130 kPa (1.3 bar), temperature −37 ° C.) flows. Then, it is fed to the scrub column 15 where the heavy fraction is separated. Then, after being cooled by the main heat exchanger 16 through which the mixed refrigerant of the second refrigeration cycle flows, the temperature is further adiabatically expanded by the expansion valve 17 to decrease the temperature, and is cooled to −162 ° C. to be liquefied and liquefied. 18 is sent.

  On the other hand, in the first refrigeration cycle, after the propane refrigerant collected from each of the heat exchangers 11, 13, 14 and the chillers 24, 25, 26 is pressurized to 1.6 MPa (16 bar) in the C3 compressor 20, The C3 compressor desuperheater 21 is cooled to 47 ° C. close to the condensation temperature by heat exchange with the cooling water, and further cooled by the C3 condenser 22 by heat exchange with the cooling water and completely condensed. The condensed propane refrigerant is further cooled by the C3 subcooler 23 and reduced to a predetermined pressure by the expansion valves 27 to 32, and then to each of the heat exchangers 11, 13, 14 and the chillers 24 to 26. Sent.

  In the second refrigeration cycle, the mixed refrigerant heat-exchanged with natural gas in the main heat exchanger 16 is compressed in two stages by the MR compressors 40 and 42, and the low-pressure stage MR compressor after cooler 41 and the high-pressure stage MR compressor are compressed. Aftercooler 43 cools to 45 ° C. with cooling water. This pressurized mixed refrigerant is sequentially heat-exchanged in chillers 24 to 26 through which propane refrigerant depressurized in three stages flows, finally cooled to -35 ° C., and partially condensed. Then, it is separated into gas and liquid by the separation drum 44 and flows into the main heat exchanger 16. The mixed refrigerant that has flowed into the main heat exchanger 16 is adiabatically expanded by the expansion valves 45 and 47 to decrease the temperature, and is sprayed from the nozzles 46 and 48 into the main heat exchanger 16. The sprayed mixed refrigerant is cooled by exchanging heat with natural gas while exchanging heat with the mixed refrigerant flowing through the pipe in the main heat exchanger 16.

  FIG. 12 is a schematic diagram showing one embodiment of the arrangement of the LNG manufacturing facility. Table 1 shows the correspondence between the device numbers and device names of the devices shown in FIG.

  Specifically, FIG. 12 shows the arrangement of a pipe rack, a C3 compressor gas turbine (C3 GT), and an MR compressor gas turbine (MR GT) in the center of the LNG production facility. FIG. A plurality of AFCs are installed at the top of the pipe rack. The size of each device relatively indicates the size of the area occupied by the actual device.

  As shown in FIG. 12, among the AFCs used in the LNG manufacturing facility, a C3 compressor desuperheater (051-E-1001: C3 Compressor Desuperheater), a C3 capacitor (051-E-1002: C3 condenser), a C3 subcooler (051-E-1003: C3 Subcooler), low pressure stage MR compressor aftercooler (051-E-1004: LP MR compressor aftercooler), high pressure stage MR compressor aftercooler (051-E-1006: HP MR compressor aftercooler), The pipe rack occupies a large area. All of these AFCs are used for liquefaction, and since the heat transfer area (heat exchange amount) is large, the effect of the desalted water spray is also increased. In particular, since the C3 capacitor occupies the largest area, if the heat transfer amount (heat exchange amount) of the C3 capacitor fluctuates, the amount of LNG produced will be significantly affected.

  Therefore, in the present embodiment, from the viewpoint of the occupied area of the equipment, the AFC for spraying demineralized water is preferably a C3 compressor desuperheater, a C3 condenser, a C3 subcooler, a low pressure stage MR compressor after cooler, and a high pressure stage MR compressor. An aftercooler, particularly preferably a C3 capacitor.

  Purified natural gas, which is a process fluid, is cooled from room temperature to around −30 ° C. by propane, and then cooled to around −162 ° C. by a mixed refrigerant through main heat exchange to become an LNG product. The mixed refrigerant is also cooled from room temperature to near −30 ° C. with propane and then supercooled through the main heat exchanger.

  Thus, since both the process fluid and the mixed refrigerant must be cooled to about −30 ° C. by propane, a decrease in the heat exchange amount of propane greatly affects the amount of LNG produced. Propane is boosted by the C3 compressor 20 and then completely condensed by the C3 condenser 22 to cool the process fluid and the mixed refrigerant to around −30 ° C. using the latent heat of vaporization. Since the condensation temperature of propane depends on the intake air temperature of the C3 condenser 22, when the intake air temperature increases due to the influence of HAR, the pressure increase by the compressor also increases, leading to energy loss.

  Therefore, in the present embodiment, from the viewpoint of the process, the AFC for spraying the demineralized water is preferably the C3 capacitor 22, and particularly preferably, the influence of the HAR is particularly large among the C3 capacitors 22 made of a plurality of AFCs. AFC.

FIG. 13 is a schematic view showing an embodiment of a demineralized water supply apparatus.
The desalted water supply device 70 has a plurality of spray nozzles 59, and the desalted water sprayed through the spray nozzles 59 evaporates to cool the cooling air of the AFC. The desalted water is supplied from the desalted water tank 50 through a foreign substance removing strainer 51, a feed water pump 52, a feed water shutoff valve 53, a feed water flow rate adjusting valve 54, a water flow meter 55, and a foreign substance removing filter 56. It is supplied to a water supply header 57 that leads to the piping. Desalinated water is supplied from the feed header 57 to the desalted water pipe via the feed header outlet flow rate adjustment valve 58, and the desalted water is sprayed through the plurality of spray nozzles 59. The sprayed demineralized water is accompanied by the air sucked by the AFC 61 and sucked upward. The sucked-up demineralized water evaporates while passing between the tubes 60 installed on the pipe rack and being discharged from the upper part of the AFC 61.
A signal of the feed water flow rate measured by the water flow meter 55 is transmitted to the control device 62, and the control device 62 can calculate the necessary water amount from the operating state of the AFC 61 and control the feed water flow rate adjustment valve 54.

  By applying the desalted water supply device shown in FIG. 13 to a specific AFC such as a C3 condenser, the desalted water is sprayed from the lower part of the AFC.

  Most LNG production facilities are built in deserts and wildernesses with gas fields, and the surrounding environment is generally hot and air is dry. During the daytime when it is lit by the sun, the tendency is stronger, and the maximum temperature reaches around 35 ° C. The difference between the daytime dry bulb temperature (air temperature) and the wet bulb temperature is often around 10 ° C, while the dew point at which water vapor condenses is lower than the wet bulb temperature. There is a possibility that the air temperature can be lowered to around 10 ° C. to the wet bulb temperature by adiabatic cooling by evaporation of salt water. It can be seen that adiabatic cooling of the AFC intake air by demineralized water spray according to the present invention is very effective.

Example 2
FIG. 14 is a schematic view showing another embodiment of the liquefaction facility in the LNG production facility. This process sequentially uses propane, ethylene, and methane as refrigerants, and is also called a cascade system.

  FIG. 14 shows a flow of natural gas (or LNG) as a process fluid (indicated by a thin solid line), a propane cooling cycle (indicated by a two-dot chain line) using propane as a working fluid, and ethylene as a working fluid. An ethylene cooling cycle (indicated by a dotted line) and a methane cooling cycle (indicated by a thick solid line) using methane as a working fluid are shown. The propane, ethylene, and methane flows constitute independent closed loops that are circulated by the compressor drive. A gas turbine and a motor (not shown) for driving the compressor are connected to the propane compressor 200, the ethylene compressor 300, and the methane compressor 400, respectively.

The main components of the propane cooling cycle are a propane compressor 200, a propane cooler 201, an expansion valve 202, a high pressure intake line 203, an intermediate pressure intake line 204, and a low pressure intake line 205.
The main components of the ethylene cooling cycle are an ethylene compressor 300, an ethylene cooler 301, an expansion valve 302, a high pressure intake line 303, and a low pressure intake line 304.
The main components of the indirect heat exchange part of the methane cooling cycle are a methane compressor 400, a methane cooler 401, a high pressure intake line 402, a medium pressure intake line 403, and a low pressure intake line 404.

Purified natural gas 100 from which typical impurities CO ₂ , H ₂ S, and water have been removed is sent to a liquefaction facility as a process fluid, and three consecutive heat exchangers having different temperatures, specifically propane, are supplied. It is cooled and liquefied by a heat exchanger 101 used as a refrigerant, a heat exchanger 102 using ethylene as a refrigerant, and a heat exchanger 103 using methane as a refrigerant. The LNG product is sent to the storage tank 105 by the pump 104 and stored until shipment. The gas slightly warmed in the storage tank and vaporized from LNG is returned to the process again, liquefied again in the heat exchanger 103, and sent to the storage tank 105 by the pump 104.

  In the propane cooling cycle, the propane refrigerant collected from the intake lines 203, 204, 205 is pressurized by the propane compressor 200, cooled by the propane cooler 201, and reduced to a predetermined pressure by the expansion valve 202. Then, it is sent to the heat exchanger 101. In the heat exchanger 101, the purified natural gas 100 and the ethylene refrigerant and methane refrigerant used in the subsequent heat exchanger are cooled by heat exchange with the propane refrigerant.

  In the ethylene cooling cycle, the ethylene refrigerant collected from the intake lines 303 and 304 is pressurized in the ethylene compressor 300, then cooled by the ethylene cooler 301, and further cooled by heat exchange with the propane refrigerant in the heat exchanger 101. Is done. Next, the pressure is reduced to a predetermined pressure by the expansion valve 302 and then sent to the heat exchanger 102. In the heat exchanger 102, the purified natural gas 100 output from the heat exchanger 101 and the methane refrigerant used in the subsequent heat exchanger are cooled by heat exchange with the ethylene refrigerant.

  In the methane cooling cycle, methane refrigerant collected from the intake lines 402, 403, and 404 is pressurized by the methane compressor 400 and then cooled by the methane cooler 401. The methane refrigerant is further cooled by heat exchange with the propane refrigerant in the heat exchanger 101, then cooled by heat exchange with the ethylene refrigerant in the heat exchanger 102, and sent to the heat exchanger 103. In the heat exchanger 103, the purified natural gas 100 output from the heat exchanger 102 is cooled and liquefied by heat exchange with the methane refrigerant.

  The fuel gas 405 is a combustible gas that contains a large amount of nitrogen and has not been liquefied. This fuel gas is used as fuel for the gas turbine that drives the compressor. However, when a large amount of power is required for LNG production, the amount of fuel gas increases and the amount of liquefied gas decreases. By increasing the heat exchange amount of AFC by spraying with desalted water, the power of the gas turbine can be reduced and the LNG production amount can be maximized.

  In the embodiment shown in FIG. 14, the AFC for spraying demineralized water according to the present invention is preferably a propane cooler 201. Spraying of demineralized water is performed using the demineralized water supply apparatus shown in FIG.

  The liquefied gas production apparatus and the liquefied gas production method of the present invention can be suitably used in the production of LNG, LPG, and SNG.

10 refined natural gas, 11 heat exchanger, 12 drums, 13 heat exchanger, 14 heat exchanger, 15 scrub column, 16 main heat exchanger, 17 expansion valve, 18 LNG tank, 20 propane (C3) compressor, 21 C3 Compressor desuperheater, 22 C3 condenser, 23 C3 subcooler, 24 chiller, 25 chiller, 26 chiller, 27 expansion valve, 28 expansion valve, 29 expansion valve, 30 expansion valve, 31 expansion valve, 32 expansion valve, 40 Low pressure stage mixing Refrigerant (MR) compressor, 41 Low pressure stage MR compressor after cooler, 42 High pressure stage MR compressor, 43 High pressure stage MR compressor after cooler, 44 Separation drum, 45 Expansion valve, 46 nozzle, 47 Expansion valve, 48 nozzle, 50 Demineralized water tank , 51 Strainer for removing foreign matter, 52 Water supply pump, 53 Water supply shutoff valve, 54 Water supply flow rate adjustment valve, 55 Water flow meter, 56 Foreign matter removal filter, 57 Water supply header, 58 Water supply header outlet flow rate adjustment valve, 59 Nozzle, 60 tube, 61 AFC, 62 Controller, 70 Demineralized water supply device, 80 Demineralized water production device, 100 Purified natural gas, 101 Heat exchanger, 102 Heat exchanger, 103 Heat exchanger, 104 Pump, 105 Storage tank, 200 Propane compressor, 201 Propane cooler, 202 Expansion valve , 203 High-pressure intake line, 204 Medium-pressure intake line, 205 Low-pressure intake line, 300 Ethylene compressor, 301 Ethylene cooler, 302 Expansion valve, 303 High-pressure intake line, 304 Low-pressure intake line, 400 Methane compressor, 401 Methane cooler, 402 High-pressure intake IN, 403 medium pressure intake line, 404 low pressure intake line, 100A air fin cooler, 100B gas turbine, 101A suction part (not shown), 101B suction part, 102A heat exchanger, 102B operation part, 103A discharge part (not shown) ), 103B discharge part (chimney), 110A compressor, 120 cooling device

Claims (10)

A liquefied gas production facility for producing a liquefied gas by liquefying from a supply gas mainly composed of methane,
A first heat exchanger that cools the supply gas and the second refrigerant by heat exchange with the first refrigerant;
A first refrigerant compressor that cools the supply gas and the second refrigerant in the first heat exchanger and compresses the gasified first refrigerant;
A second heat exchanger for further cooling and liquefying the supply gas cooled by the first heat exchanger by heat exchange with the second refrigerant;
A second refrigerant compressor that cools the supply gas in the second heat exchanger and compresses the gasified second refrigerant;
A first refrigerant air-cooled heat exchanger that cools the first refrigerant gas by cooling the first refrigerant gas discharged from the first refrigerant compressor with air;
A first refrigerant air-cooled condenser that liquefies the first refrigerant by cooling the first refrigerant gas cooled by the first refrigerant air-cooled heat exchanger with air;
A second refrigerant air-cooled heat exchanger that cools the second refrigerant gas by cooling the second refrigerant gas discharged from the second refrigerant compressor with air;
A second refrigerant air-cooled condenser that liquefies the first refrigerant by cooling the second refrigerant gas cooled by the second refrigerant air-cooled heat exchanger with air;
The first refrigerant air-cooled heat exchanger, the second refrigerant air-cooled heat exchanger, the first refrigerant air-cooled condenser, and the second refrigerant air-cooled condenser are identified so as to increase the production amount of the liquefied gas. A liquefied gas production facility comprising a mist spraying device for spraying mist composed of demineralized water onto cooling air supplied to an air-cooled heat exchanger or an air-cooled condenser and cooling the cooling air.   The liquefied gas production facility according to claim 1, wherein the specified air-cooled heat exchanger or air-cooled condenser includes a first refrigerant air-cooled condenser. An acid gas removing device for removing the acid gas in the supply gas with an amine solution;
A demineralized water production apparatus for producing demineralized water to dilute the amine solution,
The liquefied gas production apparatus according to claim 1 or 2, wherein the demineralized water constituting the mist is supplied from the demineralized water production apparatus. The specified air-cooled heat exchanger or air-cooled condenser includes
By calculating with a three-dimensional hydrodynamic equation, the weather field information of the nearby space where the liquefied gas production apparatus is arranged is calculated, and the influence of hot air recirculation (HAR) is large using the weather field information. The liquefied gas production facility according to any one of claims 1 to 3, wherein an air-cooled heat exchanger or an air-cooled condenser is included. Meteorological information set related to a plurality of times within a predetermined period in a first region including a location where the air utilization device is arranged, from a plurality of weather information including at least temperature data and related to the area and time Select multiple
Using the selected plurality of weather information sets as input data, solving a differential equation of the weather information according to an analysis model for weather simulation is related to a plurality of narrower second regions in the first region. Generate multiple first narrow-area weather information sets,
Of the plurality of generated first narrow area weather information sets, select a second narrow area weather information set for the second area including the location,
The said 2nd narrow area weather information is computed by a three-dimensional fluid dynamics formula, The weather field information of the near space where the said liquefied gas manufacturing apparatus is arrange | positioned is calculated in any one of Claims 1-4. The liquefied gas production facility described. A liquefied gas production method for producing a liquefied gas by liquefying from a supply gas mainly composed of methane,
Cooling the supply gas and the second refrigerant by heat exchange with the first refrigerant in the first heat exchanger;
In the first refrigerant compressor, cooling the supply gas and the second refrigerant in the first heat exchanger and compressing the gasified first refrigerant;
In the second heat exchanger, the supply gas cooled by the first heat exchanger is further cooled and liquefied by heat exchange with the second refrigerant;
In the second refrigerant compressor, cooling the supply gas in the second heat exchanger and compressing the gasified second refrigerant;
In the first refrigerant air-cooled heat exchanger, cooling the first refrigerant gas discharged from the first refrigerant compressor with air to cool the first refrigerant gas;
In the first refrigerant air-cooled condenser, cooling the first refrigerant gas cooled by the first refrigerant air-cooled heat exchanger with air to liquefy the first refrigerant;
Cooling the second refrigerant gas discharged from the second refrigerant compressor with air in the second refrigerant air-cooled heat exchanger; and cooling the second refrigerant gas;
A second refrigerant air-cooled condenser, wherein the second refrigerant gas cooled by the second refrigerant air-cooled heat exchanger is cooled by air to liquefy the first refrigerant;
The first refrigerant air-cooled heat exchanger, the second refrigerant air-cooled heat exchanger, the first refrigerant air-cooled condenser, and the second refrigerant air-cooled condenser are identified so as to increase the production amount of the liquefied gas. A method for producing a liquefied gas, comprising: spraying a mist composed of demineralized water on cooling air supplied to an air-cooling heat exchanger or an air-cooling condenser, and cooling the cooling air.   The liquefied gas manufacturing method according to claim 6, wherein the specified air-cooled heat exchanger or air-cooled condenser includes a first refrigerant air-cooled condenser. In the acid gas removal device, the step of removing the acid gas in the supply gas with an amine solution;
A demineralized water production apparatus comprising: a step of producing demineralized water to dilute the amine solution;
The liquefied gas manufacturing method according to claim 6 or 7, wherein the desalted water constituting the mist is supplied from the desalted water manufacturing apparatus. The specified air-cooled heat exchanger or air-cooled condenser includes
By calculating with a three-dimensional hydrodynamic equation, the weather field information of the nearby space where the liquefied gas production apparatus is arranged is calculated, and the influence of hot air recirculation (HAR) is large using the weather field information. The method for producing a liquefied gas according to any one of claims 6 to 8, wherein an air-cooled heat exchanger or an air-cooled condenser is included. Meteorological information set related to a plurality of times within a predetermined period in a first region including a location where the air utilization device is arranged, from a plurality of weather information including at least temperature data and related to the area and time Select multiple
Using the selected plurality of weather information sets as input data, solving a differential equation of the weather information according to an analysis model for weather simulation is related to a plurality of narrower second regions in the first region. Generate multiple first narrow-area weather information sets,
Of the plurality of generated first narrow area weather information sets, select a second narrow area weather information set for the second area including the location,
The second narrow area weather information is calculated by a three-dimensional hydrodynamic equation, and meteorological field information in a nearby space where the liquefied gas production apparatus is arranged is calculated according to any one of claims 6 to 9. The liquefied gas manufacturing method of description.