CN105865149B - A method of producing liquid air using cold energy of liquefied natural gas - Google Patents

A method of producing liquid air using cold energy of liquefied natural gas Download PDF

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CN105865149B
CN105865149B CN201610255613.9A CN201610255613A CN105865149B CN 105865149 B CN105865149 B CN 105865149B CN 201610255613 A CN201610255613 A CN 201610255613A CN 105865149 B CN105865149 B CN 105865149B
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air
nitrogen
heat exchanger
cold energy
cryogenic
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CN105865149A (en
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熊永强
罗鹏
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Jinan University
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Jinan University
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0012—Primary atmospheric gases, e.g. air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
    • F25J3/04024—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of purified feed air, so-called boosted air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/004—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by flash gas recovery
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
    • F25J1/0052—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
    • F25J1/007—Primary atmospheric gases, mixtures thereof
    • F25J1/0072—Nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0203—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a single-component refrigerant [SCR] fluid in a closed vapor compression cycle
    • F25J1/0208—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a single-component refrigerant [SCR] fluid in a closed vapor compression cycle in combination with an internal quasi-closed refrigeration loop, e.g. with deep flash recycle loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0221—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using the cold stored in an external cryogenic component in an open refrigeration loop
    • F25J1/0222—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using the cold stored in an external cryogenic component in an open refrigeration loop in combination with an intermediate heat exchange fluid between the cryogenic component and the fluid to be liquefied
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
    • F25J1/0235—Heat exchange integration
    • F25J1/0242—Waste heat recovery, e.g. from heat of compression
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0244—Operation; Control and regulation; Instrumentation
    • F25J1/0245—Different modes, i.e. 'runs', of operation; Process control
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
    • F25J1/0262—Details of the cold heat exchange system
    • F25J1/0264—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams
    • F25J1/0265—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams comprising cores associated exclusively with the cooling of a refrigerant stream, e.g. for auto-refrigeration or economizer
    • F25J1/0268—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams comprising cores associated exclusively with the cooling of a refrigerant stream, e.g. for auto-refrigeration or economizer using a dedicated refrigeration means
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
    • F25J1/0292—Refrigerant compression by cold or cryogenic suction of the refrigerant gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04254—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using the cold stored in external cryogenic fluids
    • F25J3/0426—The cryogenic component does not participate in the fractionation
    • F25J3/04266—The cryogenic component does not participate in the fractionation and being liquefied hydrocarbons
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/62—Liquefied natural gas [LNG]; Natural gas liquids [NGL]; Liquefied petroleum gas [LPG]
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/04—Compressor cooling arrangement, e.g. inter- or after-stage cooling or condensate removal
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/30—Compression of the feed stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • F25J2270/904—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by liquid or gaseous cryogen in an open loop

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

The invention belongs to cold energy of liquefied natural gas to utilize technical field, disclose a kind of method producing liquid air using cold energy of liquefied natural gas.This method includes following steps：(1) air compression and purification；(2) air liquefaction；(3) nitrogen is for SAPMAC method；(4) coolant media Rankine cycle；(5) heated by natural gas；(6) compressed air of LNG cold energy is utilized to cool down.The flowage structure of the method for the present invention is the principle based on cascaded utilization of energy, LNG cold energy is orderly used to liquefaction of nitrogen, nitrogen precooled, coolant media Rankine cycle and the cooling of compressed air according to temperature from low to high, realize that the cascade utilization of LNG cold energy, utilization ratio are high.This method is used for the liquefaction of air using nitrogen as the cold energy of dielectric film filter LNG, improves liquefied fraction, and can avoid air and liquefied natural gas direct heat transfer, the safety of raising system, also, this method is adapted to the fluctuation of liquefied natural gas gasifying amount, has preferable operation flexible.

Description

A method of producing liquid air using cold energy of liquefied natural gas
Technical field
The invention belongs to cold energy of liquefied natural gas to utilize technical field, more particularly to a kind of to be given birth to using cold energy of liquefied natural gas The method for producing liquid air.
Background technology
With the fast development of China's economic society, to energy demand rapid development, in order to meet the country to clean energy resource Great demand, China is since 2006 from external a large amount of Liquefied Natural Gas Imports (LNG).Currently, at present in Guangdong, good fortune It builds, Zhejiang, Shanghai, Jiangsu, Shandong, Hebei, Liaoning, Guangxi, coastal provinces and cities' planning such as Tianjin and Hainan and built multiple LNG Project, annual LNG import volumes have reached 19,890,000 tons within 2014.The LNG of import is a kind of -162 DEG C of atmospheric low-temperature liquid, After LNG is pressurized to 7~10MPa (absolute pressure, the pressure appeared below are absolute pressure) using pump in receiving station, then Heated vaporization could be supplied to downstream user to use into gas ductwork.Conventional LNG vaporization method is in open-shelf vaporization In device (ORV) or vaporizer (IFV) with intermediate heat transfer media using seawater as heat source by LNG heating vaporizations, in winter A part of natural gas is then burnt to heat vapour in temperature and the lower area of ocean temperature in submerged combustion type vaporizer (SCV) Change LNG, not only a large amount of valuable cold energy are taken away by seawater in this way, cause huge energy waste, but also can be to Vaporizing Station week The water ecological setting on side causes apparent cold pollution.
LNG cold energy is a kind of very good clean energy resource, and natural gas needs to consume a large amount of electricity during liquefied It can be used to freeze, can release about 230KWh/t cold energy when vaporization.LNG cold energy can be used for air separation, low temperature Freezer, waste old low-temperature grinding etc. reduce the energy consumption needed for refrigeration, but the amount needed for these cold energy use modes is smaller, The evaporating capacity of much smaller than the one annual millions of tons of LNG receiving stations.LNG cold energy is transformed into electricity using cold energy generation facility Can, be it is a kind of can be by large-scale recovery in the way of receiving station's cold energy, and industrial chain is most short, and institute's generated energy can be for LNG Receiving station is personal or surfs the Internet, and is not interfered by factors such as market, resource environment, transports.But the efficiency of LNG cold energy generations It is relatively low, general only 30% or so.
The utilization ratio of LNG cold energy is related to the temperature utilized, lower using temperature, then cold energy use efficiency is higher. Therefore, LNG cold energy is used to produce the liquid air of deep cooling, higher cold energy use efficiency can be not only obtained, avoid LNG vapour The cold pollution caused by surrounding enviroment of change process, and the energy consumption of liquid air can be greatly reduced, promote liquid air The development of downstream industry chain.Currently, greatly developing the peak load regulation network technology using liquid air, liquid air vapour both at home and abroad The green energy resources technology such as vehicle dynamical system, the application market of liquid air are very extensive.But due to conventional air liquefaction process Irreversibility it is larger, liquid air energy consumption is excessively high, and this greatly limits the large-scale applications of these new technologies.
The domestic liquid air production technology announced includes mainly at present：
(1) Chinese utility model patent 201220370879.5 describes a kind of high-pressure liquid air energy storage/release system, High pressure is compressed air to using compressor in energy storage subsystem, the cold energy and air for then recycling regenerator to store are through low The cold energy that temperature expansion generates liquefies pressure-air, and is stored in high pressure low temperature storage tank, realizes high-pressure liquid air energy storage.
(2) Chinese utility model patent 201220370906.9 describes a kind of efficient high-pressure liquid air energy storage release System is equally to compress air to high pressure using compressor in energy storage subsystem, then recycles the cold of regenerator storage The cold energy that can be generated with air low temperature expansion liquefies pressure-air, and is stored in high pressure low temperature storage tank, and recycles air The work(that cryogenic expansion machine generates drives air compressor, improves efficiency of energy utilization.
It is that high pressure is compressed air to by compressor in above two patented technology, it is then swollen by air again Swollen refrigeration or regenerator cooling produce liquid air.It is on the one hand no in compression process due to air to carry out cascade EDFA, Air is compressed at a higher temperature, causes the energy consumption of air compressor very high, and the irreversible loss of process is big.It is another Aspect needs more pressure-air that pressure-air could liquefy by cryogenic expansion machine swell refrigeration, the liquid of raw air Rate is relatively low, and the energy consumption of liquid air is higher.
(3) Chinese invention patent application number 201310279616.2 discloses a kind of nuclear power peak regulation system based on deep cooling energy storage Low power consumption phase extra electricity is driven air compressor in air liquefaction subsystem wherein, compressed air to by system High pressure recycles the cold energy that low-pressure low-temperature air and cold-storage unit after expansion provide to be cooled to lower temperature, then passes through The decompression of low temperature turbine is freezed to generate liquid air, and extra nuclear power is stored in liquid air.In that patent, a part of Cryogenic air is used for the cascade EDFA of air compression process, can reduce the energy consumption of air compressor.But the patent is to take Pressure-air generates liquid air through low temperature turbine expansion, the air fluid rate of system on the one hand can be caused relatively low, another party The humidity of face low temperature turbine exhaust is larger, is unfavorable for the safe operation of equipment.
(4) Chinese invention patent application number 201310388410.3 describes a kind of liquid air energy-storage system, wherein wrapping It is used for air-fluidized subsystem containing a kind of cold energy using cool storage medium storage LNG vaporization release, but is not directed to specifically such as What produces the technological process of liquid air using LNG cold energy.
From above-mentioned existing patented technology it is found that production liquefied air is required for air being compressed to higher pressure, liquid The energy consumption of state air production process is essentially from air compression process.In addition, conventional liquid air production process is due to needing There is provided a part of pressure-air low-temperature expansion to the cold energy needed for air liquefaction, therefore the air fluid rate of system is relatively low.
Invention content
In order to overcome the shortcomings and deficiencies of the prior art described above, it liquefies the primary purpose of the present invention is that providing a kind of utilize The method that natural gas cold energy produces liquid air.On the one hand, the liquefaction of air is used for using nitrogen as the cold energy of dielectric film filter LNG, Air-fluidized pressure is reduced, air fluid rate is improved, and can avoid air and liquefied natural gas direct heat transfer, improves system Safety；Second aspect, using the LNG cold energy in circulating refrigerant recycling higher temperature section, between the grade of air compressor It is cooling, reduce the energy consumption of air compression process；In terms of third, using system integration technology, one is devised with circulating refrigerant For the low temperature Rankine cycle of working medium, using compressed air as heat source, LNG is low-temperature receiver, and a part of LNG cold energy is converted to power, is carried High-energy source utilization ratio.
The purpose of the present invention is realized by following proposal：
A method of producing liquid air, including operating procedure in detail below using cold energy of liquefied natural gas：
(1) air compression and purification
Air initially enters self-cleaning air intake filter device 1, removes dust contained in air and its in the filter It is mixed using the non-liquefied air flowed out in mixer 3 and from cryogenic heat exchanger 11 after flow valve 2 after its granule foreign It closes, then through air compressor 4,6 and 8 is compressed to 0.5MPa or so step by step (absolute pressure, the pressure appeared below are absolute pressure Power).The compressed air being discharged from air compressor 8 is cooled to slightly below room temperature through aerial cooler 9, subsequently into air purification Water, carbon dioxide and some hydrocarbons in air are removed in device 10, become drying compressed air stream.
(2) air liquefaction
The drying compressed air stream obtained in step (1) enters in cryogenic heat exchanger 11, through with flowed out from flow valve 21 Liquid nitrogen, the low temperature nitrogen in cryogenic heat exchanger 18, and the Cryogenic air flowed out from liquid air storage tank 13 exchange heat.It is dry Compressed air stream all liquefies after absorbing cold energy, then is sent into liquid air storage tank 13 after the decompression of cryogenic throttle valve 12.From liquid The bottom of state air reservoir 13 can get the liquid air product of required pressure, and the Cryogenic air that pressure reduction generates is then from liquid The top of state air reservoir 13 is discharged, then returns in mixing valve 3 after cryogenic heat exchanger 11 recycles cold energy and mixed with raw air. On the other hand, liquid nitrogen and the low temperature nitrogen from cryogenic heat exchanger 18 are heated in cryogenic heat exchanger 11, and liquid nitrogen all gasifies, Temperature increases, and then this two strands of nitrogen remix and constitute cyclic nitrogen air-flow in mixing valve 22.
(3) nitrogen is for SAPMAC method
The normal pressure liquefied natural gas (LNG) that need to be vaporized is forced into 7~10MPa by LNG pump 23, becomes high pressure LNG, temperature About -145~-156 DEG C；The cyclic nitrogen air-flow obtained in step (2) exchanges heat in cryogenic heat exchanger 14 with high pressure LNG, will follow Ring nitrogen is cooled to -100 DEG C or so, then recycles nitrogen compressor 15,16 and 17 that circulating nitrogen gas is compressed to high pressure step by step. In order to reduce the energy consumption of nitrogen compressor, circulating nitrogen gas utilizes height before entering nitrogen compressor in cryogenic heat exchanger 14 Pressure LNG is cooled to -100 DEG C or so in advance.From nitrogen compressor 17 come out cycle of higher pressure nitrogen again in cryogenic heat exchanger 14 with height LNG heat exchange, temperature is pressed to be reduced to the high pressure LNG than entering cryogenic heat exchanger 14 about 2~5 DEG C high.Cycle of higher pressure nitrogen after cooling Gas is further cooling through cryogenic heat exchanger 18 again, is then sent into liquid nitrogen storage tank 20 after the decompression of cryogenic throttle valve 19.Reducing pressure by regulating flow The low temperature nitrogen of generation is separated from the top of liquid nitrogen storage tank 20, after cryogenic heat exchanger 18 exchanges heat recovery section cold energy, is entered back into It exchanges heat with compressed air in cryogenic heat exchanger 11.And the liquid nitrogen obtained in 20 bottom of liquid nitrogen storage tank then passes through flow valve 21 and adjusts stream Enter cryogenic heat exchanger 11 after amount, required cold energy is provided for air liquefaction.Liquid nitrogen all gasifies after heat exchange, then through mixing valve 22 It is mixed into cyclic nitrogen air-flow with another strand of nitrogen flowed out from cryogenic heat exchanger 11, constitutes nitrogen for SAPMAC method.At the same time, The high pressure LNG flowed out from cryogenic heat exchanger 14 has all gasified, and becomes cryogenic high pressure natural gas flow.
(4) coolant media Rankine cycle
The cryogenic high pressure natural gas flow obtained in step (3) enters in cryogenic heat exchanger 24 to exchange heat with circulating refrigerant, cycle Refrigerant all liquefies after absorbing cold energy, becomes liquid coolant.Liquid coolant enters cryogenic heat exchanger after the supercharging of refrigerant pump 26 again It exchanges heat with one hot glycol water in 27；After heat exchange, hot glycol water is cooled to 0~5 DEG C, becomes low temperature second two Alcohol solution；Liquid coolant after supercharged also all gasifies simultaneously, then seawater or low temperature exhaust heat are utilized in cryogenic heat exchanger 28 Cold media gas is heated to 5 DEG C or more, is depressured subsequently into being expanded in refrigerant expanding machine 29, the cold media gas after expansion returns again to It liquefies in cryogenic heat exchanger 24, forms a coolant media Rankine cycle.The power of coolant media Rankine cycle output can be used In driving air compressor or nitrogen compressor, the power consumption of system is reduced.
(5) heated by natural gas
The high-pressure natural gas temperature flowed out from the cryogenic heat exchanger 24 described in step (4) is still below 0 DEG C, is inputted low It is heated to 0 DEG C or more using seawater or other low temperature exhaust heats in warm heat exchanger 25, finally enters gas distributing system.
(6) compressed air of LNG cold energy is utilized to cool down
In the low-temperature glycol aqueous solution that step (4) obtains after 30 supercharging of glycol water pump, then through flow divider 31 It is divided into three strands with 32, is respectively fed to be used for the cascade EDFA of air compression process in heat exchanger 5 and 7, and be sent into air cooling The cooling of compressed air is used in device 9.After heat exchange, the temperature of glycol water is increased to 15~30 DEG C, then through mixing valve 33 It is mixed into one hot glycol water with 34, then returns again to cryogenic heat exchanger 27, forms cold energy use cycle.Compression is empty During air cooling, there is partial moisture that can condense out, is discharged by the condensate outlet of heat exchanger 5,7 and 9.
Wherein, in step (1) in order to reduce the energy consumption of air compression process grade is set up between air compressor 4,6 and 8 Between cooler 5 and 7, using low-temperature glycol aqueous solution as low-temperature receiver carry out cascade EDFA.
The air is cooled to using low-temperature glycol aqueous solution between 5~10 DEG C in interstage cooler.
Wherein, the mixing valve 3 in step (1) is used for the non-liquefied air that is returned from cryogenic heat exchanger 11 and air raw material Mixing, in order to reduce the energy consumption of air compressor, air raw material isobaric as possible should be mixed with the non-liquefied air returned；Work as return Non- liquefied air pressure close to normal pressure when, then mixing valve 3 is placed in before air compressor 4；When the non-liquefied air pressure of return When power is higher, then mixing valve 3 can be placed according to the non-liquefied air pressure size of return after interstage cooler 5 or 7.
Circulating nitrogen gas described in step (3) is compressed to 6.0MPa or more step by step through nitrogen compressor 15,16 and 17.
Cryogenic throttle valve 19 described in step (3) is for regulating and controlling liquid nitrogen storage tank and entering cryogenic heat exchanger 11 for air liquefaction The pressure of the liquid nitrogen of cold energy is provided, the outlet pressure of cryogenic throttle valve 19 is low compared with the outlet pressure of air compressor 8 0.02~ 0.11MPa。
Flow valve 2 and 21 described in step (1) and (3) is respectively used to regulation and control into the air capacity and circulating nitrogen gas of system Amount, when the LNG amounts for entering system increase or reduce, regulating flow quantity valve 2 and 21 carrys out the air liquefaction amount of regulating system and follows Ring nitrogen amount makes system have stronger operation flexible.
Coolant media described in step (4) is carbon dioxide, propane, ammonia, monochlorodifluoromethane, dichlorodifluoromethane, two Fluoroethane, tetrafluoroethane, freon R410A etc..
Refrigerant pump 26 described in step (4), output pressure should make the bubble point temperature of coolant media at 0 DEG C or so.
The present invention compared with the existing technology, has the following advantages and advantageous effect：
(1) flowage structure of the invention is the principle based on cascaded utilization of energy, LNG cold energy according to temperature from low to high according to It is secondary to be used for liquefaction of nitrogen, nitrogen precooled, coolant media Rankine cycle and the cooling of compressed air, realize the ladder of LNG cold energy Grade utilizes, and cold energy use is more efficient.
(2) present invention employ nitrogen as intermediate medium come utilize LNG cold energy produce liquid air, avoid air with LNG direct heat transfers, the safety higher of system.
(3) present invention is using LNG cold energy as low-temperature receiver, for air liquefaction and air compression process cascade EDFA provide it is cold Can, so that the cold energy of LNG is stored in liquid air with higher efficiency, reduces the wave of LNG gasification process cold energy Take, and the power consumption of the production of liquid air can be greatly reduced, the more conventional liquid air of production power consumption of liquid air per ton Production method can reduce by 65% or more.
(4) present invention can adjust air liquefaction amount by the way that flow valve 2 and 21 is arranged according to the LNG amounts for entering system With cyclic nitrogen tolerance, changed by the liquid level of liquid nitrogen storage tank to adjust the produce load of liquid air, to adapt to LNG gasification amount Fluctuation, make system have preferable operation flexible.
Description of the drawings
Fig. 1 is the work flow diagram of the present invention.
Fig. 2 is another work flow diagram of the present invention.
Wherein：
Specific device numbering：
1- self-cleaning air intake filter devices；2,21- flow valves；
3,22,33,34- mixing valves；4,6,8- air compressors；
5,7,9- aerial coolers；10- air purifiers；
11,14,18,24,25,27,28- cryogenic heat exchangers；
12,19- cryogenic throttle valves；
13- liquid air storage tanks；15,16,17- nitrogen compressors；
20- liquid nitrogen storage tanks；23- liquefied natural gas pumps；
26- refrigerant pumps；29- refrigerant expanding machines；
30- glycol waters pump；31,32- flow dividers；
Logistics illustrates：
Specific implementation mode
With reference to embodiment and attached drawing, the present invention is described in further detail, but embodiments of the present invention are unlimited Routine techniques progress can refer to for not specifically specified technological parameter in this.
Embodiment 1：
As shown in Figure 1, a kind of method producing liquid air using cold energy of liquefied natural gas includes the following steps and technique Condition：
Liquefied natural gas (LNG) mole group of receiving station becomes：Methane 88.78%, ethane 7.54%, propane 2.59%, Iso-butane 0.45%, butane 0.56%, nitrogen 0.08%；LNG gasification amount is 180t/h, and air-treatment amount is 100t/h, and Rankine follows The coolant media that ring selects is carbon dioxide.
It is as follows：
(1) air compression and purification
Normal pressure, 15 DEG C of air raw material enter self-cleaning air intake filter device 1, remove in the filter contained in air Dust and other granule foreigns after, using flow valve 2 by air input control be 100t/h；Air raw material is in mixer It is thoroughly mixed with the non-liquefied air about 16.87t/h flowed out from cryogenic heat exchanger 11 in 3, then through air compressor 4,6 and 8 It is compressed to 0.5MPa step by step, the compression ratio of every air compressor is set as 1.71.In order to reduce the energy consumption of air compression process, Interstage cooler 5 and 7 is set up between three air compressors, (quality of glycol content is using 0 DEG C of glycol water 25%) compressed air is cooled to 7 DEG C.The 0.5MPa compressed airs being discharged from air compressor 8 utilize 0 DEG C in heat exchanger 9 Glycol water be cooled to 10 DEG C, subsequently into air purifier 10 remove air in water, carbon dioxide and some Hydrocarbon becomes drying compressed air stream, and temperature is about 15 DEG C, and pressure is about 0.49MPa, and flow is about 116.17t/ h。
(2) air liquefaction
The drying compressed air stream obtained in step (1) enters in cryogenic heat exchanger 11, through with exported from flow valve 21 118.1t/h liquid nitrogen (- 179.8 DEG C, 0.47MPa), in cryogenic heat exchanger 18 55.9t/h low temperature nitrogens (- 152 DEG C, 0.47MPa), and from liquid air storage tank 13 (- 150 DEG C, the 0.47MPa) heat exchange of 16.87t/h Cryogenic airs flowed out.It is dry Compressed air stream all liquefies after absorbing cold energy, then liquid air storage tank is sent into after cryogenic throttle valve 12 is depressurized to 0.11MPa In 13.Liquid air product 99.3t/h (- 193.3 DEG C, 0.11MPa) is can get from the bottom of liquid air storage tank 13, and is depressured The 16.87t/h Cryogenic airs (- 193.3 DEG C, 0.11MPa) that process generates then are discharged from the top of liquid air storage tank 13, then pass through After cryogenic heat exchanger 11 recycles cold energy, temperature is increased to 10 DEG C, is then back in mixing valve 3 and is mixed with air raw material.Another party Face, 118.1t/h liquid nitrogen and the 55.9t/h low temperature nitrogens from cryogenic heat exchanger 18 exchange heat in cryogenic heat exchanger 11, and liquid nitrogen is complete Portion gasifies, and temperature is increased to -66.5 DEG C, and then this two strands of nitrogen remix and constitute cyclic nitrogen air-flow, flow in mixing valve 22 For 174t/h.
(3) nitrogen is for SAPMAC method
The normal pressure LNG about 180t/h that need to be vaporized are forced into 7.0MPa by LNG pump 23, become high pressure LNG, are changed into low temperature Temperature when hot device 14 is about -153 DEG C；The 174t/h cyclic nitrogens air-flow obtained in step (2) in cryogenic heat exchanger 14 with height Press LNG heat exchange, circulating nitrogen gas is cooled to -103 DEG C, then recycle nitrogen compressor 15,16 and 17 by circulating nitrogen gas step by step It is compressed to 7.5MPa, the compression ratio of every nitrogen compressor is equal, and about 2.55.In order to reduce the energy consumption of nitrogen compressor, Circulating nitrogen gas is cooled to -103 DEG C in advance in cryogenic heat exchanger 14 before entering nitrogen compressor using high pressure LNG.From nitrogen The cycle of higher pressure nitrogen (7.5MPa, -39.1 DEG C) that compressor 17 comes out exchanges heat in cryogenic heat exchanger 14 with high pressure LNG again, temperature Degree is reduced to -151 DEG C, becomes high-pressure liquid nitrogen, then -155.0 DEG C is cooled further to through cryogenic heat exchanger 18 again, then low Warm throttle valve 19 is depressurized to 0.47MPa and is re-fed into liquid nitrogen storage tank 20.The 55.9t/h low temperature nitrogens that reducing pressure by regulating flow generates (0.47MPa, -179.8 DEG C) is separated from the top of liquid nitrogen storage tank 20, after cryogenic heat exchanger 18 exchanges heat recovery section cold energy, temperature Degree is increased to -152 DEG C, enters back into cryogenic heat exchanger 11 and exchanges heat with compressed air.And the liquid obtained in 20 bottom of liquid nitrogen storage tank Nitrogen then enters cryogenic heat exchanger 11 after flow valve 21, and flow 118.1t/h provides required cold energy for air liquefaction.It changes Liquid nitrogen all gasifies after heat, then is mixed into circulating nitrogen gas with another strand of nitrogen flowed out from cryogenic heat exchanger 11 through mixing valve 22 Stream, temperature are increased to -65.3 DEG C, constitute nitrogen for SAPMAC method.At the same time, the high pressure LNG flowed out from cryogenic heat exchanger 14 is Through whole gasifications, temperature is increased to -55.1 DEG C, and pressure reduction to 6.8MPa becomes cryogenic high pressure natural gas flow, and flow is 180t/h。
(4) coolant media Rankine cycle
The cryogenic high pressure natural gas flow obtained in step (3) enter in cryogenic heat exchanger 24 with circulating refrigerant medium 71.4t/ H carbon dioxide (- 37.0 DEG C of temperature, pressure 1.1MPa, vapour phase fraction 0.92) exchanges heat, whole liquid after carbon dioxide absorption cold energy Change, becomes carbon dioxide liquid.Carbon dioxide liquid enters after pressure is promoted to 3.7MPa by refrigerant pump 26 from 1.05MPa again In cryogenic heat exchanger 27 with the heat exchange of (25.1 DEG C) of the glycol water of one 272.4t/h；After heat exchange, glycol water temperature Degree is reduced to 0 DEG C, becomes low-temperature glycol aqueous solution；Liquid CO 2 after supercharged also all gasifies simultaneously, and temperature increases To 2.0 DEG C, then carbon dioxide is heated to 10 DEG C using seawater in cryogenic heat exchanger 28, subsequently into refrigerant expanding machine 29 It is expanded to 1.1MPa, the carbon dioxide gas after expansion is returned again in cryogenic heat exchanger 24 and liquefied, and it is bright to form a coolant media Agree cycle.The net work of coolant media Rankine cycle output is about 570kW, can be used for driving air compressor or nitrogen compression Machine reduces the power consumption of system.
(5) heated by natural gas
The high-pressure natural gas temperature flowed out from the cryogenic heat exchanger 24 described in step (4) is increased to -41 DEG C, is inputted It is heated to 0 DEG C or more using seawater or other low temperature exhaust heats in cryogenic heat exchanger 25, pressure reduction to 6.6MPa finally enters day Right gas pipe network.
(6) compressed air of LNG cold energy is utilized to cool down
Step (4) obtain 272.4t/h, 0 DEG C of low-temperature glycol aqueous solution through glycol water pump 30 from After 0.15MPa is pressurized to 0.30MPa, then through flow divider 31 and 32 it is divided into three strands, one 98.3t/h is sent into heat exchanger 5, one 86.9t/h is sent into heat exchanger 7 cascade EDFA for being used for air compression process, and also one 87.2t/h is sent into heat exchanger 9 and uses In the cooling of compressed air.After heat exchange, the temperature of glycol water is increased to 25.1 DEG C, then is mixed into through mixing valve 33 and 34 For one hot glycol water, cryogenic heat exchanger 27 is then returned again to, forms cold energy use cycle.Compressed air cooling procedure In, there is partial moisture that can condense out, is discharged by the condensate outlet of heat exchanger 5,7 and 9.
During entire air liquefaction, the cold energy that is discharged using the high pressure LNG gasification of 180t/h can produce 99.3t/h, The liquid air of 0.11MPa, total system power consumption are 14531kW (deducting the work(that coolant media Rankine cycle generates), averagely produce 1 The power consumption of the liquid air of ton 0.11MPa is about 146.3kWh.And the power consumption that conventional method produces identical liquid air is about 439kWh/t, thus using it is proposed by the present invention it is a kind of using LNG cold energy production liquid air method come produce liquid air can The power consumption for saving 66.7% can have good energy-saving effect using the cold energy of 1 ton of LNG releases with using electricity wisely 161.5kWh.
Embodiment 2：
As shown in Fig. 2, a kind of method producing liquid air using cold energy of liquefied natural gas includes the following steps and technique Condition：
Liquefied natural gas (LNG) mole group of receiving station becomes：Methane 96.64%, ethane 2.77%, propane 0.34%, Iso-butane 0.07%, butane 0.08%, nitrogen 0.10%；LNG gasification amount is 120t/h, and air-treatment amount is 67t/h, Rankine cycle The coolant media selected is tetrafluoroethane.
It is as follows：
(1) air compression and purification
Normal pressure, 15 DEG C of air raw material enter self-cleaning air intake filter device 1, remove in the filter contained in air Dust and other granule foreigns after, using flow valve 2 by air input control be 67t/h.Air raw material is through air pressure Contracting machine 4 and 6 is compressed to 0.33MPa step by step, and the compression ratio of every air compressor is set as 1.81, then in mixer 3 with from The non-liquefied air about 4.69t/h flowed out in cryogenic heat exchanger 11 is thoroughly mixed, then again through air compressor 8 by air into one Step is compressed to 0.6MPa.In order to reduce the energy consumption of air compression process, interstage cooler 5 is set up between three air compressors With 7, compressed air is cooled to 5 DEG C using 0 DEG C of glycol water (quality of glycol content about 25%).It is compressed from air The 0.6MPa compressed airs that machine 8 is discharged are cooled to 10 DEG C in heat exchanger 9 using 0 DEG C of glycol water, subsequently into sky Water, carbon dioxide and some hydrocarbons in air are removed in gas purifier 10, become drying compressed air stream, temperature About 15 DEG C, pressure is about 0.59MPa, and flow is about 71.22t/h.
(2) air liquefaction
The drying compressed air stream obtained in step (1) enters in cryogenic heat exchanger 11, through with exported from flow valve 21 72.2t/h liquid nitrogen (- 177.8 DEG C, 0.55MPa), in cryogenic heat exchanger 18 39.8t/h low temperature nitrogens (- 177.8 DEG C, 0.55MPa), and from liquid air storage tank 13 (- 150 DEG C, the 0.47MPa) heat exchange of 4.69t/h Cryogenic airs flowed out.Dry pressure Stream of compressed air all liquefies after absorbing cold energy, then liquid air storage tank 13 is sent into after cryogenic throttle valve 12 is depressurized to 0.34MPa In.Liquid air product 66.53t/h (- 181.8 DEG C, 0.34MPa) is can get from the bottom of liquid air storage tank 13, and is depressured The 4.69t/h Cryogenic airs that process generates then are discharged from the top of liquid air storage tank 13, then recycle through cryogenic heat exchanger 11 cold After energy, temperature is increased to 10 DEG C, is then back in mixing valve 3 and is mixed with raw air.On the other hand, 72.2t/h liquid nitrogen and come It exchanging heat in cryogenic heat exchanger 11 from the 39.8t/h low temperature nitrogens of cryogenic heat exchanger 18, liquid nitrogen all gasifies, and temperature is increased to- 59.0 DEG C, then this two strands of nitrogen remix and constitute cyclic nitrogen air-flow, flow 112t/h in mixing valve 22.
(3) nitrogen is for SAPMAC method
The normal pressure LNG about 120t/h that need to be vaporized are forced into 10.0MPa by LNG pump 23, become high pressure LNG, input low temperature Temperature when heat exchanger 14 is about -150 DEG C；The 112t/h cyclic nitrogens air-flow obtained in step (2) in cryogenic heat exchanger 14 with High pressure LNG heat exchange, circulating nitrogen gas are cooled to -100 DEG C, then recycle nitrogen compressor 15,16 and 17 by circulating nitrogen gas by Grade is compressed to 6.5MPa, and the compression ratio of every nitrogen compressor is equal, and about 2.29.In order to reduce the energy of nitrogen compressor Consumption, circulating nitrogen gas are cooled to -100 DEG C in advance in cryogenic heat exchanger 14 before entering nitrogen compressor using high pressure LNG.From nitrogen The cycle of higher pressure nitrogen (6.5MPa, -36.3 DEG C) that air compressor 17 comes out exchanges heat in cryogenic heat exchanger 14 with high pressure LNG again, Temperature is reduced to -148 DEG C, becomes high-pressure liquid nitrogen, is then cooled further to -152.0 DEG C through cryogenic heat exchanger 18 again, then exists Cryogenic throttle valve 19 is depressurized to 0.55MPa and is re-fed into liquid nitrogen storage tank 20.The 39.8t/h low temperature nitrogens that reducing pressure by regulating flow generates (0.55MPa, -177.8 DEG C) is separated from the top of liquid nitrogen storage tank 20, after cryogenic heat exchanger 18 exchanges heat recovery section cold energy, temperature Degree is increased to -150 DEG C, enters back into cryogenic heat exchanger 11 and exchanges heat with compressed air.And the liquid obtained in 20 bottom of liquid nitrogen storage tank Nitrogen then enters cryogenic heat exchanger 11 after flow valve 21, and flow 72.2t/h provides required cold energy for air liquefaction.It changes Liquid nitrogen all gasifies after heat, then is mixed into circulating nitrogen gas with another strand of nitrogen flowed out from cryogenic heat exchanger 11 through mixing valve 22 Stream constitutes nitrogen for SAPMAC method, and temperature is about -59 DEG C.At the same time, the high pressure LNG flowed out from cryogenic heat exchanger 14 is complete Portion gasifies, and temperature is increased to -60.6 DEG C, and pressure reduction to 9.8MPa becomes cryogenic high pressure natural gas flow, flow 120t/h.
(4) coolant media Rankine cycle
The cryogenic high pressure natural gas flow obtained in step (3) enter in cryogenic heat exchanger 24 with circulating refrigerant medium 61t/h Tetrafluoroethane gas (- 9.4 DEG C of temperature, pressure 0.06MPa) exchanges heat, and tetrafluoroethane gas all liquefies after absorbing cold energy, becomes Tetrafluoroethane liquid.Tetrafluoroethane liquid changes after pressure is promoted to 0.31MPa by refrigerant pump 26 from 0.04MPa into low temperature again (20.0 DEG C, quality of glycol content is 25%) to exchange heat with the glycol water of one 221.6t/h in hot device 27；After heat exchange, Glycol water temperature is reduced to 0 DEG C, becomes low-temperature glycol aqueous solution；Liquid tetrafluorethane after supercharged is also whole simultaneously Gasification, temperature is increased to -1.1 DEG C, then tetrafluoroethane gas is heated to 25 DEG C using low temperature exhaust heat in cryogenic heat exchanger 28, Subsequently into 0.06MPa is expanded in refrigerant expanding machine 29, the tetrafluoroethane gas after expansion returns again in cryogenic heat exchanger 24 Liquefaction forms a coolant media Rankine cycle.The net work of coolant media Rankine cycle output is about 415.6kW, be can be used for Air compressor or nitrogen compressor are driven, the power consumption of system is reduced.
(5) heated by natural gas
The high-pressure natural gas temperature flowed out from the cryogenic heat exchanger 24 described in step (4) is increased to -39.3 DEG C, its is defeated Enter in cryogenic heat exchanger 25 and be heated to 0 DEG C or more using seawater or other low temperature exhaust heats, pressure reduction to 9.6MPa finally enters Gas distributing system.
(6) compressed air of LNG cold energy is utilized to cool down
Step (4) obtain 221.6t/h, 0 DEG C of low-temperature glycol aqueous solution through glycol water pump 30 from After 0.15MPa is pressurized to 0.30MPa, then through flow divider 31 and 32 it is divided into three strands, one 84.3t/h is sent into heat exchanger 5, one 69t/h is sent into heat exchanger 7 cascade EDFA for being used for air compression process, and also one 68.3t/h is sent into heat exchanger 9 and is used for The cooling of compressed air.After heat exchange, the temperature of glycol water is increased to 20 DEG C, then is mixed into one through mixing valve 33 and 34 The hot glycol water of stock, then returns again to cryogenic heat exchanger 27, forms cold energy use cycle.In compressed air cooling procedure, There is partial moisture that can condense out, is discharged by the condensate outlet of heat exchanger 5,7 and 9.
During entire air liquefaction, the cold energy that is discharged using the high pressure LNG gasification of 120t/h can produce 66.53t/h, The liquid air of 0.34MPa, total system power consumption are 8737kW (deducting the work(that coolant media Rankine cycle generates), averagely produce 1 The power consumption of the liquid air of ton 0.34MPa is about 131.3kWh.And the power consumption that conventional method produces identical liquid air is about 400kWh/t, thus it is proposed by the present invention it is a kind of using LNG cold energy production liquid air method can be saved to produce liquid air 67.2% power consumption can have good energy-saving effect using the cold energy of 1 ton of LNG releases with using electricity wisely 149kWh.
The above embodiment is a preferred embodiment of the present invention, but embodiments of the present invention are not by above-described embodiment Limitation, it is other it is any without departing from the spirit and principles of the present invention made by changes, modifications, substitutions, combinations, simplifications, Equivalent substitute mode is should be, is included within the scope of the present invention.

Claims (8)

1. a kind of method producing liquid air using cold energy of liquefied natural gas, it is characterised in that including operating step in detail below Suddenly：
(1) air compression and purification
Air initially enters self-cleaning air intake filter device (1), removes dust and other contained in air in the filter After granule foreign, using the outflow in the first mixing valve (3) and from the first cryogenic heat exchanger (11) after first flow valve (2) Non- liquefied air mixing, then through the first air compressor (4), the second air compressor (6) and third air compressor (8) by Grade is compressed to 0.5MPa；The compressed air being discharged from third air compressor (8) is cooled to slightly below often through aerial cooler (9) Temperature becomes dry pressure subsequently into water, carbon dioxide and some hydrocarbons in removing air in air purifier (10) Stream of compressed air；
(2) air liquefaction
The drying compressed air stream obtained in step (1) enters in the first cryogenic heat exchanger (11), through with from second flow valve (21) liquid nitrogen, the low temperature nitrogen in third cryogenic heat exchanger (18) flowed out, and flowed out from liquid air storage tank (13) Cryogenic air heat exchange；Drying compressed air stream all liquefies after absorbing cold energy, then after the first cryogenic throttle valve (12) decompression It is sent into liquid air storage tank (13)；The liquid air product of pressure needed for being obtained from the bottom of liquid air storage tank (13), and The Cryogenic air that pressure reduction generates then is discharged from the top of liquid air storage tank (13), then is returned through the first cryogenic heat exchanger (11) It returns after receipts cold energy and is mixed with raw air in the first mixing valve (3)；On the other hand, liquid nitrogen and come from third cryogenic heat exchanger (18) low temperature nitrogen is heated in the first cryogenic heat exchanger (11), and liquid nitrogen all gasifies, and temperature increases, then mixed second It closes this two strands of nitrogen in valve (22) and remixes composition cyclic nitrogen air-flow；
(3) nitrogen is for SAPMAC method
The normal pressure liquefied natural gas (LNG) that need to be vaporized is forced into 7~10MPa by LNG pump (23), becomes high pressure LNG, temperature It is -145~-156 DEG C；The cyclic nitrogen air-flow obtained in step (2) exchanges heat in the second cryogenic heat exchanger (14) with high pressure LNG, Circulating nitrogen gas is cooled to -100 DEG C, then recycles the first nitrogen compressor (15), the second nitrogen compressor (16) and third Circulating nitrogen gas is compressed to high pressure by nitrogen compressor (17) step by step；In order to reduce the energy consumption of nitrogen compressor, circulating nitrogen gas into It is cooled to -100 DEG C in advance using high pressure LNG in the second cryogenic heat exchanger (14) before entering nitrogen compressor；From third nitrogen pressure The cycle of higher pressure nitrogen that contracting machine (17) comes out exchanges heat in the second cryogenic heat exchanger (14) with high pressure LNG again, and temperature is reduced to ratio Into 2~5 DEG C of the high pressure LNG high of the second cryogenic heat exchanger (14)；Cycle of higher pressure nitrogen after cooling is again through third low-temperature heat exchange Device (18) is further cooling, is then sent into liquid nitrogen storage tank (20) after the second cryogenic throttle valve (19) decompression；Reducing pressure by regulating flow generates Low temperature nitrogen separated at the top of liquid nitrogen storage tank (20), through third cryogenic heat exchanger (18) exchange heat recovery section cold energy after, then It exchanges heat into the first cryogenic heat exchanger (11) with compressed air；And the liquid nitrogen obtained in liquid nitrogen storage tank (20) bottom then passes through the Two flow valves (21) enter the first cryogenic heat exchanger (11) after adjusting flow, and required cold energy is provided for air liquefaction；After heat exchange Liquid nitrogen all gasifies, then is mixed into another strand of nitrogen flowed out from the first cryogenic heat exchanger (11) through the second mixing valve (22) Cyclic nitrogen air-flow constitutes nitrogen for SAPMAC method；At the same time, the high pressure LNG flowed out from the second cryogenic heat exchanger (14) is complete Portion gasifies, and becomes cryogenic high pressure natural gas flow；
(4) coolant media Rankine cycle
The cryogenic high pressure natural gas flow obtained in step (3) enters in the 4th cryogenic heat exchanger (24) to exchange heat with circulating refrigerant, follows Ring refrigerant all liquefies after absorbing cold energy, becomes liquid coolant；It is low that liquid coolant enters the 6th after refrigerant pump (26) supercharging again It exchanges heat with one hot glycol water in warm heat exchanger (27)；After heat exchange, hot glycol water is cooled to 0~5 DEG C, at For low-temperature glycol aqueous solution；Liquid coolant after supercharged also all gasifies simultaneously, then the profit in the 7th cryogenic heat exchanger (28) Cold media gas is heated to 5 DEG C or more with seawater or low temperature exhaust heat, subsequently into expansion decompression in refrigerant expanding machine (29), expansion Cold media gas afterwards returns again to liquefaction in the 4th cryogenic heat exchanger (24), forms a coolant media Rankine cycle；Coolant media The power of Rankine cycle output reduces the power consumption of system for driving air compressor or nitrogen compressor；
(5) heated by natural gas
The high-pressure natural gas temperature flowed out from the 4th cryogenic heat exchanger (24) described in step (4) is still below 0 DEG C, is inputted It is heated to 0 DEG C or more using seawater or other low temperature exhaust heats in 5th cryogenic heat exchanger (25), finally enters gas distributing system；
(6) compressed air of LNG cold energy is utilized to cool down
In the low-temperature glycol aqueous solution that step (4) obtains after glycol water pump (30) supercharging, then through the first flow divider (31) and the second flow divider (32) is divided into three strands, is respectively fed in the first interstage cooler (5) and the second interstage cooler (7) For the cascade EDFA of air compression process, and the cooling for being used for compressed air is sent into aerial cooler (9)；After heat exchange, The temperature of glycol water is increased to 15~30 DEG C, then is mixed into one through third mixing valve (33) and the 4th mixing valve (34) The hot glycol water of stock, then returns again to the 6th cryogenic heat exchanger (27), forms cold energy use cycle；Compressed air is cooled Cheng Zhong has partial moisture that can condense out, by the first interstage cooler device (5), the second interstage cooler (7) and air cooling The condensate outlet of device (9) is discharged.
2. the method according to claim 1 for producing liquid air using cold energy of liquefied natural gas, it is characterised in that：Step (1) first air compressor (4) is set up between the second air compressor (6) and third air compressor (8) between the first order Cooler (5) and the second interstage cooler (7) carry out cascade EDFA using low-temperature glycol aqueous solution as low-temperature receiver.
3. the method according to claim 2 for producing liquid air using cold energy of liquefied natural gas, it is characterised in that：It is described First interstage cooler (5) and the second interstage cooler (7) cool air to 5~10 DEG C.
4. the method according to claim 1 for producing liquid air using cold energy of liquefied natural gas, it is characterised in that：When returning When the non-liquefied air pressure returned is close to normal pressure, then the first mixing valve (3) described in step (1) is placed in the first air compressor (4) before；When the non-liquefied air pressure of return is higher, then the first mixing valve (3) described in step (1) is placed between the first order After cooler (5) or the second interstage cooler (7).
5. the method according to claim 1 for producing liquid air using cold energy of liquefied natural gas, it is characterised in that：Step (3) circulating nitrogen gas described in is through the first nitrogen compressor (15), the second nitrogen compressor (16) and third nitrogen compressor (17) It is compressed to 6.0MPa or more step by step.
6. the method according to claim 1 for producing liquid air using cold energy of liquefied natural gas, it is characterised in that：Step (3) outlet pressure of the second cryogenic throttle valve (19) described in is low compared with the outlet pressure of third air compressor (8) 0.02~ 0.11MPa。
7. the method according to claim 1 for producing liquid air using cold energy of liquefied natural gas, it is characterised in that：Step (4) coolant media described in is carbon dioxide, propane, ammonia, monochlorodifluoromethane, dichlorodifluoromethane, Difluoroethane, tetrafluoro second Alkane or freon R410A.
8. the method according to claim 1 for producing liquid air using cold energy of liquefied natural gas, it is characterised in that：Step (4) refrigerant pump (26) its output pressure described in makes the bubble point temperature of coolant media at 0 DEG C.
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