CN105865149A - Method for producing liquid air by utilizing liquefied natural gas cold energy - Google Patents

Method for producing liquid air by utilizing liquefied natural gas cold energy Download PDF

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Publication number
CN105865149A
CN105865149A CN201610255613.9A CN201610255613A CN105865149A CN 105865149 A CN105865149 A CN 105865149A CN 201610255613 A CN201610255613 A CN 201610255613A CN 105865149 A CN105865149 A CN 105865149A
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air
nitrogen
heat exchanger
cold energy
cryogenic
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CN105865149B (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
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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
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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
    • 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]
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    • 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
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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
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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
    • 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 the technical field of LNG (Liquefied Natural Gas) cold energy utilization and discloses a method for producing liquid air by utilizing LNG cold energy. The method comprises the following steps: (1) air compression and purification; (2) air liquefaction; (3) nitrogen cooling cycle; (4) cooling medium Rankine cycle; (5) natural gas heating; and (6) compressed air cooling based on the LNG cold energy. According to the method provided by the invention, the flow structure is based on a principle of cascaded utilization of energy, the LNG cold energy is used for nitrogen liquefaction, nitrogen precooling, cooling medium Rankine cycle and compressed air cooling in sequence from low temperature to high temperature, cascaded utilization of the LNG cold energy is realized, and the utilization efficiency is high. According to the method, nitrogen is taken as a medium to recycle the LNG cold energy for air liquefaction, the liquefaction ratio is increased, direct heat exchange between air and the LNG can be avoided, the system safety is improved; and the method can be adapted to fluctuation of LNG gasification quantity and has good operation flexibility.

Description

A kind of method utilizing cold energy of liquefied natural gas to produce liquid air
Technical field
The invention belongs to cold energy of liquefied natural gas and utilize technical field, utilize cold energy of liquefied natural gas raw particularly to one The method producing liquid air.
Background technology
Along with the fast development of China's economic society, to energy demand rapid development, domestic to clean energy resource in order to meet Great demand, China started from external a large amount of Liquefied Natural Gas Import (LNG) from 2006.At present, the most in Guangdong, good fortune Build, Zhejiang, Shanghai, Jiangsu, Shandong, Hebei, Liaoning, Guangxi, the coastal provinces and cities planning such as Tianjin and Hainan and built multiple LNG Project, within 2014, annual LNG import volume has reached 19,890,000 tons.The LNG of import is the atmospheric low-temperature liquid of a kind of-162 DEG C, After utilizing pump that LNG is pressurized to 7～10MPa (absolute pressures, the pressure appeared below is absolute pressure) in receiving station, then Heated vaporization could enter gas ductwork and be supplied to downstream user to use.Conventional LNG vaporization method is in open-shelf vaporization LNG heating is vaporized, in the winter time by device (ORV) or carburator (IFV) the interior employing sea water with intermediate heat transfer media as thermal source Temperature and ocean temperature lower ground district, then a part of natural gas that burns in submerged combustion type carburator (SCV) heats vapour Changing LNG, the most a large amount of valuable cold energy are taken away by sea water, cause huge energy waste, but also can be to Vaporizing Station week The water ecological setting on limit causes obvious cold pollution.
LNG cold energy is the clean energy resource of a kind of very high-quality, and natural gas needs to consume substantial amounts of electricity during liquefaction Can be used for freezing, vaporization when, releasably go out about 230KW h/t cold energy.LNG cold energy may be used for air separation, low temperature The aspects such as freezer, waste old low-temperature grinding reduce the energy consumption needed for refrigeration, but the amount needed for these cold energy use modes is less, Evaporating capacity much smaller than an annual millions of tons of LNG receiving station.Utilize cold energy generation facility that LNG cold energy is transformed into electricity Can, be a kind of can be in the way of large-scale recovery utilizes receiving station's cold energy, and industrial chain is the shortest, and institute's generated energy can be for LNG Receiving station is personal or surfs the Net, and is not disturbed by the such as factor such as market, resource environment, transport.But the efficiency of LNG cold energy generation Relatively low, general only about 30%.
The utilization ratio of LNG cold energy is relevant to the temperature utilized, and utilizes temperature the lowest, then cold energy use efficiency is the highest. Therefore, LNG cold energy is used for producing the liquid air of deep cooling, is possible not only to obtain higher cold energy use efficiency, it is to avoid LNG vapour The cold pollution that surrounding enviroment are caused by change process, and the energy consumption of liquid air can be greatly reduced, promote liquid air The development of downstream industry chain.At present, the most greatly developing and utilizing the peak load regulation network technology of liquid air, liquid air vapour The green energy resource technology such as car dynamical system, the application market of liquid air is widely.But due to conventional air liquefaction process Irreversibility relatively big, liquid air energy consumption is too high, this greatly limits the large-scale application of these new techniques.
The most domestic liquid air production technology announced specifically includes that
(1) Chinese utility model patent 201220370879.5 describes a kind of high-pressure liquid air energy storage/release system, Utilizing compressor to compress air to high pressure in energy storage subsystem, the cold energy of then recycling regenerator storage and air are through low Temperature expands the cold energy produced and is liquefied by pressure-air, and is stored in high pressure low temperature storage tank, it is achieved 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 to utilize compressor to compress air to high pressure in energy storage subsystem equally, and then the storage of recycling regenerator is cold The cold energy produced can be expanded with air low temperature to be liquefied by pressure-air, and be stored in high pressure low temperature storage tank, and reclaim air The merit that cryogenic expansion machine produces drives air compressor, improves efficiency of energy utilization.
In above two patented technology, it is all to compress air to high pressure by compressor, swollen by air the most again Swollen refrigeration or regenerator cooling produce liquid air.On the one hand in compression process, interstage cooling is not carried out due to air, Air is compressed the most at a higher temperature, and the energy consumption causing air compressor is the highest, and the irreversible loss of process is big.Another Aspect, needs more pressure-air could be liquefied by pressure-air 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 of based on deep cooling energy storage peak regulation system System, drives air compressor by the electricity unnecessary the low power consumption phase in air liquefaction subsystem wherein, compresses air to High pressure, the cold energy recycling the low-pressure low-temperature air after expanding and the offer of cold-storage unit is cooled to lower temperature, then warp Low temperature turbine blood pressure lowering refrigeration produces liquid air, is stored in liquid air by unnecessary nuclear power.In that patent, a part Cryogenic air, for the interstage cooling of air compression process, can reduce the energy consumption of air compressor.But this patent is to take Pressure-air produces liquid air through low temperature turbine expansion, and the air fluid rate that on the one hand can cause system is relatively low, the opposing party The humidity of face low temperature turbine exhaust is relatively big, 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 wraps Containing a kind of cold energy utilizing cool storage medium storage LNG vaporization to discharge for air-fluidized subsystem, but it is not directed to the most such as What utilizes LNG cold energy to produce the technological process of liquid air.
Knowable to above-mentioned existing patented technology, produce liquefied air and be required for being compressed to air higher pressure, liquid The energy consumption of state air production process is essentially from air compression process.Additionally, the liquid air production process of routine is due to needs A part of pressure-air low-temperature expansion provides the cold energy needed for air liquefaction, and therefore the air fluid rate of system is relatively low.
Summary of the invention
In order to overcome the shortcoming of above-mentioned prior art with not enough, the primary and foremost purpose of the present invention is that providing a kind of utilizes liquefaction sky The method that so air cooling can produce liquid air.On the one hand, with nitrogen be dielectric film filter LNG cold energy for the liquefaction of air, reduce Air-fluidized pressure, improves air fluid rate, and can avoid air and liquefied natural gas direct heat transfer, improve the safety of system Property；Second aspect, utilizes circulating refrigerant to reclaim the LNG cold energy that higher temperature is interval, for the interstage cooling of air compressor, reduces The energy consumption of air compression process；3rd aspect, utilizes system integration technology, devises the low temperature with circulating refrigerant as working medium Rankine cycle, with compressed air as thermal source, LNG is low-temperature receiver, and a part of LNG cold energy is converted to power, improves efficiency of energy utilization.
The purpose of the present invention is realized by following proposal:
A kind of method utilizing cold energy of liquefied natural gas to produce liquid air, including operating procedure in detail below:
(1) air compression and purification
Air initially enters self-cleaning air intake filter device 1, remove in the filter dust contained in air and its After its granule foreign, the more non-liquefied air flowed out in blender 3 and from cryogenic heat exchanger 11 after flow valve 2 mixes Close, then (absolute pressure, the pressure appeared below is absolute pressure to be compressed to about 0.5MPa step by step through air compressor 4,6 and 8 Power).The compressed air discharged from air compressor 8 is cooled to slightly below room temperature through air cooler 9, subsequently into air cleaning Device 10 removes water, carbon dioxide and some Hydrocarbon in air, becomes dry compressed air stream.
(2) air liquefaction
The dry compressed air stream obtained in step (1) enters in cryogenic heat exchanger 11, through with flow out from flow valve 21 Liquid nitrogen, from the low temperature nitrogen in cryogenic heat exchanger 18, and the Cryogenic air heat exchange flowed out from liquid air storage tank 13.It is dried Compressed air stream all liquefies after absorbing cold energy, then sends in liquid air storage tank 13 after cryogenic throttle valve 12 blood pressure lowering.From liquid The bottom of state air reservoir 13 can obtain the liquid air product of desirable pressure, and the Cryogenic air that pressure reduction produces is then from liquid The top of state air reservoir 13 is discharged, then mixes with raw air in return mixing valve 3 after cryogenic heat exchanger 11 reclaims cold energy. 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 raises, and then in mixing valve 22, these two strands of nitrogen remix composition cyclic nitrogen air-flow.
(3) nitrogen is for SAPMAC method
The normal pressure liquefied natural gas (LNG) that need to vaporize is forced into 7～10MPa by LNG pump 23, becomes high pressure LNG, temperature It is about-145～-156 DEG C；The cyclic nitrogen air-flow obtained in step (2) in cryogenic heat exchanger 14 with high pressure LNG heat exchange, will follow Ring nitrogen is cooled to about-100 DEG C, and then circulating nitrogen gas is compressed to high pressure by recycling nitrogen compressor 15,16 and 17 step by step. In order to reduce the energy consumption of nitrogen compressor, circulating nitrogen gas all utilized height before entering nitrogen compressor in cryogenic heat exchanger 14 Pressure LNG is cooled to about-100 DEG C in advance.From nitrogen compressor 17 cycle of higher pressure nitrogen out again cryogenic heat exchanger 14 with height Pressure LNG heat exchange, the high pressure LNG that temperature is reduced to than entering cryogenic heat exchanger 14 is the highest 2～5 DEG C.Cycle of higher pressure nitrogen after cooling Gas cools down further through cryogenic heat exchanger 18 again, then sends into liquid nitrogen storage tank 20 after cryogenic throttle valve 19 blood pressure lowering.Reducing pressure by regulating flow The low temperature nitrogen produced separates from the top of liquid nitrogen storage tank 20, after cryogenic heat exchanger 18 heat exchange recovery section cold energy, enters back into With compressed air heat exchange in cryogenic heat exchanger 11.The liquid nitrogen obtained bottom liquid nitrogen storage tank 20 is then through flow valve 21 regulation stream Cryogenic heat exchanger 11, the cold energy needed for providing for air liquefaction are provided after amount.After heat exchange, liquid nitrogen all gasifies, more blended 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.Meanwhile, The high pressure LNG flowed out from cryogenic heat exchanger 14 the most all gasifies, and becomes cryogenic high pressure natural gas flow.
(4) coolant media Rankine cycle
With circulating refrigerant heat exchange, circulation in the cryogenic high pressure natural gas flow entrance cryogenic heat exchanger 24 obtained in step (3) Coolant all liquefies after absorbing cold energy, becomes liquid coolant.Liquid coolant enters cryogenic heat exchanger again after refrigerant pump 26 supercharging With one hot glycol water heat exchange in 27；After heat exchange, hot glycol water is cooled to 0～5 DEG C, becomes low temperature second two Alcohol-water solution；Liquid coolant after supercharging the most all gasifies simultaneously, then utilizes sea water or low temperature exhaust heat in cryogenic heat exchanger 28 Cold media gas is heated to more than 5 DEG C, and subsequently into expanding blood pressure lowering in coolant decompressor 29, the cold media gas after expansion returns again to Cryogenic heat exchanger 24 liquefies, forms a coolant media Rankine cycle.The power of coolant media Rankine cycle output can be used In driving air compressor or nitrogen compressor, reduce 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 still below 0 DEG C, is inputted low Temperature heat exchanger 25 utilizes sea water or other low temperature exhaust heat to be heated to more than 0 DEG C, finally enters gas distributing system.
(6) pressure-air cooling of LNG cold energy is utilized
The low-temperature glycol aqueous solution obtained in step (4) is after glycol water pump 30 supercharging, then through flow divider 31 It is divided into three strands with 32, is respectively fed to the interstage cooling for air compression process in heat exchanger 5 and 7, and sends into air cooling For compressed-air actuated cooling in device 9.After heat exchange, the temperature of glycol water is increased to 15～30 DEG C, more blended valve 33 It is mixed into one hot glycol water with 34, then returns again to cryogenic heat exchanger 27, form cold energy use circulation.Compression sky During air cooling, there is portion of water to condense out, discharged by the condensate outlet of heat exchanger 5,7 and 9.
Wherein, in order to reduce the energy consumption of air compression process in step (1), between air compressor 4,6 and 8, level is set up Between cooler 5 and 7, utilize low-temperature glycol aqueous solution to carry out interstage cooling as low-temperature receiver.
Described air utilizes low-temperature glycol aqueous solution to be cooled between 5～10 DEG C in interstage cooler.
Wherein, mixing valve in step (1) 3 is for the non-liquefied air returned from cryogenic heat exchanger 11 and air raw material Mixing, in order to reduce the energy consumption of air compressor, air raw material should be tried one's best with the non-liquefied air of return isobaric mixing；Work as return Non-liquefied air pressure close to normal pressure time, then before mixing valve 3 is placed in air compressor 4；When the non-liquefied air pressure returned When power is higher, then after mixing valve 3 can be placed in interstage cooler 5 or 7 according to the non-liquefied air pressure size returned.
Circulating nitrogen gas described in step (3) is compressed to more than 6.0MPa step by step through nitrogen compressor 15,16 and 17.
Cryogenic throttle valve 19 described in step (3) is used for regulating and controlling liquid nitrogen storage tank and entering cryogenic heat exchanger 11 for air liquefaction The pressure of liquid nitrogen of cold energy is provided, the outlet pressure of cryogenic throttle valve 19 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 regulate and control air capacity and the circulating nitrogen gas of entrance system Amount, when the LNG amount of the system of entrance increases or reduces, regulating flow quantity valve 2 and 21 regulates the air liquefaction amount of system and follows Ring nitrogen amount, makes system have stronger operation flexible.
Coolant media described in step (4) be carbon dioxide, propane, ammonia, monochlorodifluoromethane, dichlorodifluoromethane, two Fluoroethane, tetrafluoroethane, freon R410A etc..
Refrigerant pump 26 described in step (4), its output pressure should make the bubble point temperature of coolant media at about 0 DEG C.
The present invention, relative to prior art, has such advantages as and beneficial effect:
(1) flowage structure of the present invention is principle based on cascaded utilization of energy, and LNG cold energy depends on from low to high according to temperature Secondary for liquefaction of nitrogen, nitrogen precooled, coolant media Rankine cycle and compressed-air actuated cooling, it is achieved that the ladder of LNG cold energy Level utilizes, and cold energy use is in hgher efficiency.
(2) present invention employs nitrogen as intermediate medium to utilize LNG cold energy to produce liquid air, it is to avoid air with LNG direct heat transfer, the safety of system is higher.
(3) present invention utilizes LNG cold energy to provide cold as low-temperature receiver, the interstage cooling for air liquefaction and air compression process Can, not only enable the cold energy of LNG be stored in liquid air with higher efficiency, reduce 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 more than 65%.
(4) present invention is by arranging flow valve 2 and 21, can regulate air liquefaction amount according to the LNG amount of the system of entrance With cyclic nitrogen tolerance, changed the production load regulating liquid air by the liquid level of liquid nitrogen storage tank, thus adapt to LNG gasification amount Fluctuation, make system have preferably and operate flexibility.
Accompanying drawing explanation
Fig. 1 is the workflow diagram of the present invention.
Fig. 2 is the another kind of workflow diagram of the present invention.
Wherein:
Concrete device numbering:
1-self-cleaning air intake filter device；2,21-flow valves；
3,22,33,34-mixing valves；4,6,8-air compressors；
5,7,9-air coolers；10-air purifier；
11,14,18,24,25,27,28-cryogenic heat exchangers；
12,19-cryogenic throttle valves；
13-liquid air storage tank；15,16,17-nitrogen compressors；
20-liquid nitrogen storage tank；23-liquefied natural gas pump；
26-refrigerant pump；29-coolant decompressor；
30-glycol water pump；31,32-flow dividers；
Logistics illustrates:
Detailed description of the invention
Below in conjunction with embodiment and accompanying drawing, the present invention is described in further detail, but embodiments of the present invention do not limit In this, for the technological parameter indicated the most especially, can refer to routine techniques and carry out.
Embodiment 1:
As it is shown in figure 1, a kind of method utilizing cold energy of liquefied natural gas to produce liquid air comprises the following steps and technique Condition:
The liquefied natural gas (LNG) mole of receiving station consists of: 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.
Specifically comprise the following steps that
(1) air compression and purification
Normal pressure, the air raw material of 15 DEG C enter self-cleaning air intake filter device 1, remove in air contained in the filter Dust and other granule foreign after, then through flow valve 2, air input is controlled as 100t/h；Air raw material is at blender 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 Being compressed to 0.5MPa step by step, the compression ratio of every air compressor is all set to 1.71.In order to reduce the energy consumption of air compression process, Setting up interstage cooler 5 and 7 between three air compressors, (quality of glycol content is to utilize the glycol water of 0 DEG C 25%) by pressure-air cooling to 7 DEG C.The 0.5MPa compressed air discharged from air compressor 8 utilizes 0 DEG C heat exchanger 9 Glycol water be cooled to 10 DEG C, subsequently into the water removed in air purifier 10 in air, carbon dioxide and some Hydrocarbon, becomes dry compressed air stream, and its temperature is about 15 DEG C, and pressure is about 0.49MPa, and flow is about 116.17t/ h。
(2) air liquefaction
The dry compressed air stream obtained in step (1) enters in cryogenic heat exchanger 11, through with export from flow valve 21 118.1t/h liquid nitrogen (-179.8 DEG C, 0.47MPa), from cryogenic heat exchanger 18 55.9t/h low temperature nitrogen (-152 DEG C, 0.47MPa), and from liquid air storage tank 13 16.87t/h Cryogenic air (-150 DEG C, the 0.47MPa) heat exchange flowed out.It is dried Compressed air stream all liquefies after absorbing cold energy, then sends into liquid air storage tank after cryogenic throttle valve 12 is depressurized to 0.11MPa In 13.Liquid air product 99.3t/h (-193.3 DEG C, 0.11MPa) can be obtained from the bottom of liquid air storage tank 13, and blood pressure lowering The 16.87t/h Cryogenic air (-193.3 DEG C, 0.11MPa) that process produces then is discharged from the top of liquid air storage tank 13, then warp After cryogenic heat exchanger 11 reclaims cold energy, temperature is increased to 10 DEG C, is then back in mixing valve 3 mix with air raw material.The opposing party Face, 118.1t/h liquid nitrogen and the 55.9t/h low temperature nitrogen heat exchange in cryogenic heat exchanger 11 from cryogenic heat exchanger 18, liquid nitrogen is complete Gasifying in portion, temperature is increased to-66.5 DEG C, and then in mixing valve 22, these two strands of nitrogen remix composition cyclic nitrogen air-flow, flow For 174t/h.
(3) nitrogen is for SAPMAC method
The normal pressure LNG about 180t/h that need to vaporize is forced into 7.0MPa by LNG pump 23, becomes high pressure LNG, enters low temperature and changes Temperature during hot device 14 is about-153 DEG C；The 174t/h cyclic nitrogen air-flow obtained in step (2) in cryogenic heat exchanger 14 with height Pressure LNG heat exchange, circulating nitrogen gas is cooled to-103 DEG C, and then recycling nitrogen compressor 15,16 and 17 is by circulating nitrogen gas step by step Being compressed to 7.5MPa, the compression ratio of every nitrogen compressor is the most equal, and about 2.55.In order to reduce the energy consumption of nitrogen compressor, Circulating nitrogen gas all utilized high pressure LNG to be cooled to-103 DEG C in advance before entering nitrogen compressor in cryogenic heat exchanger 14.From nitrogen Compressor 17 cycle of higher pressure nitrogen out (7.5MPa ,-39.1 DEG C) again in cryogenic heat exchanger 14 with high pressure LNG heat exchange, temperature Degree is reduced to-151 DEG C, becomes high-pressure liquid nitrogen, is cooled further to-155.0 DEG C through cryogenic heat exchanger 18 the most again, then low Temperature choke valve 19 is depressurized to 0.47MPa and is re-fed into liquid nitrogen storage tank 20.The 55.9t/h low temperature nitrogen that reducing pressure by regulating flow produces (0.47MPa ,-179.8 DEG C) separates from the top of liquid nitrogen storage tank 20, after cryogenic heat exchanger 18 heat exchange recovery section cold energy, and temperature Degree be increased to-152 DEG C, enter back in cryogenic heat exchanger 11 with compressed air heat exchange.And the liquid obtained bottom liquid nitrogen storage tank 20 Nitrogen then enters cryogenic heat exchanger 11 after flow valve 21, and flow is 118.1t/h, the cold energy needed for providing for air liquefaction.Change After heat, liquid nitrogen all gasifies, more blended valve 22 is mixed into circulating nitrogen gas with another strand of nitrogen flowed out from cryogenic heat exchanger 11 Stream, temperature is increased to-65.3 DEG C, constitutes nitrogen for SAPMAC method.Meanwhile, from the high pressure LNG of cryogenic heat exchanger 14 outflow Through all gasifications, temperature is increased to-55.1 DEG C, pressure drop as little as 6.8MPa, becomes cryogenic high pressure natural gas flow, and flow is 180t/h。
(4) coolant media Rankine cycle
With circulating refrigerant medium 71.4t/ in the cryogenic high pressure natural gas flow entrance cryogenic heat exchanger 24 obtained in step (3) H carbon dioxide (temperature-37.0 DEG C, pressure 1.1MPa, vapour phase fraction 0.92) heat exchange, whole liquid after carbon dioxide absorption cold energy Change, become carbon dioxide liquid.Pressure is entered after 1.05MPa is promoted to 3.7MPa by carbon dioxide liquid again through refrigerant pump 26 With glycol water (25.1 DEG C) heat exchange of one 272.4t/h in cryogenic heat exchanger 27；After heat exchange, glycol water temperature Degree is reduced to 0 DEG C, becomes low-temperature glycol aqueous solution；Liquid CO 2 after supercharging the most all gasifies simultaneously, and temperature raises To 2.0 DEG C, then utilize sea water that carbon dioxide is heated to 10 DEG C in cryogenic heat exchanger 28, subsequently in coolant decompressor 29 Being expanded to 1.1MPa, the carbon dioxide after expansion returns again to liquefy in cryogenic heat exchanger 24, forms a coolant media bright It agree circulation.The net work of coolant media Rankine cycle output is about 570kW, may 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 Cryogenic heat exchanger 25 utilize sea water or other low temperature exhaust heat are heated to more than 0 DEG C, pressure drop as little as 6.6MPa, finally enter sky So gas pipe network.
(6) pressure-air cooling of LNG cold energy is utilized
The 272.4t/h obtained in step (4), the low-temperature glycol aqueous solution of 0 DEG C through glycol water pump 30 from After 0.15MPa is pressurized to 0.30MPa, then being divided into three strands through flow divider 31 and 32, one 98.3t/h sends in heat exchanger 5, one 86.9t/h sends into the interstage cooling in heat exchanger 7 for air compression process, also has one 87.2t/h to send in heat exchanger 9 and uses In compressed-air actuated cooling.After heat exchange, the temperature of glycol water is increased to 25.1 DEG C, more blended valve 33 and 34 is mixed into For one hot glycol water, then return again to cryogenic heat exchanger 27, form cold energy use circulation.Pressure-air cooling process In, there is portion of water to condense out, discharged by the condensate outlet of heat exchanger 5,7 and 9.
During whole air liquefaction, the cold energy utilizing the high pressure LNG gasification of 180t/h to discharge can produce 99.3t/h, The liquid air of 0.11MPa, total system power consumption is 14531kW (merit that deduction coolant media Rankine cycle produces), averagely produces 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, therefore use the present invention propose one utilize LNG cold energy produce liquid air method to produce liquid air can Save the power consumption of 66.7%, utilize the cold energy of 1 ton of LNG release can have good energy-saving effect with using electricity wisely 161.5kWh.
Embodiment 2:
As in figure 2 it is shown, a kind of method utilizing cold energy of liquefied natural gas to produce liquid air comprises the following steps and technique Condition:
The liquefied natural gas (LNG) mole of receiving station consists of: 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.
Specifically comprise the following steps that
(1) air compression and purification
Normal pressure, the air raw material of 15 DEG C enter self-cleaning air intake filter device 1, remove in air contained in the filter Dust and other granule foreign after, then through flow valve 2, air input is controlled as 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 all set to 1.81, then in blender 3 with from The non-liquefied air about 4.69t/h flowed out in cryogenic heat exchanger 11 is thoroughly mixed, and through air compressor 8, air is entered one the most again Step is compressed to 0.6MPa.In order to reduce the energy consumption of air compression process, between three air compressors, set up interstage cooler 5 With 7, utilize the glycol water (quality of glycol content about 25%) of 0 DEG C by pressure-air cooling to 5 DEG C.Compress from air The 0.6MPa compressed air that machine 8 is discharged utilizes the glycol water of 0 DEG C to be cooled to 10 DEG C, subsequently into sky in heat exchanger 9 Gas purifier 10 removes water, carbon dioxide and some Hydrocarbon in air, becomes dry compressed air stream, its temperature Being about 15 DEG C, pressure is about 0.59MPa, and flow is about 71.22t/h.
(2) air liquefaction
The dry compressed air stream obtained in step (1) enters in cryogenic heat exchanger 11, through with export from flow valve 21 72.2t/h liquid nitrogen (-177.8 DEG C, 0.55MPa), from cryogenic heat exchanger 18 39.8t/h low temperature nitrogen (-177.8 DEG C, 0.55MPa), and from liquid air storage tank 13 4.69t/h Cryogenic air (-150 DEG C, the 0.47MPa) heat exchange flowed out.It is dried pressure Stream of compressed air all liquefies after absorbing cold energy, then sends into liquid air storage tank 13 after cryogenic throttle valve 12 is depressurized to 0.34MPa In.Liquid air product 66.53t/h (-181.8 DEG C, 0.34MPa) can be obtained from the bottom of liquid air storage tank 13, and blood pressure lowering The 4.69t/h Cryogenic air that process produces then is discharged from the top of liquid air storage tank 13, then reclaims cold through cryogenic heat exchanger 11 After energy, temperature is increased to 10 DEG C, is then back in mixing valve 3 mix with raw air.On the other hand, 72.2t/h liquid nitrogen is with next From 39.8t/h low temperature nitrogen heat exchange in cryogenic heat exchanger 11 of cryogenic heat exchanger 18, liquid nitrogen all gasifies, and temperature is increased to- 59.0 DEG C, then in mixing valve 22, these two strands of nitrogen remix composition cyclic nitrogen air-flow, and flow is 112t/h.
(3) nitrogen is for SAPMAC method
The normal pressure LNG about 120t/h that need to vaporize is forced into 10.0MPa by LNG pump 23, becomes high pressure LNG, inputs low temperature Temperature during heat exchanger 14 is about-150 DEG C；The 112t/h cyclic nitrogen air-flow obtained in step (2) in cryogenic heat exchanger 14 with High pressure LNG heat exchange, circulating nitrogen gas is cooled to-100 DEG C, then recycling nitrogen compressor 15,16 and 17 by circulating nitrogen gas by Level is compressed to 6.5MPa, and the compression ratio of every nitrogen compressor is the most equal, and about 2.29.In order to reduce the energy of nitrogen compressor Consumption, circulating nitrogen gas all utilized high pressure LNG to be cooled to-100 DEG C in advance before entering nitrogen compressor in cryogenic heat exchanger 14.From nitrogen Air compressor 17 cycle of higher pressure nitrogen out (6.5MPa ,-36.3 DEG C) again in cryogenic heat exchanger 14 with high pressure LNG heat exchange, Temperature is reduced to-148 DEG C, becomes high-pressure liquid nitrogen, is cooled further to-152.0 DEG C through cryogenic heat exchanger 18 the most 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 nitrogen that reducing pressure by regulating flow produces (0.55MPa ,-177.8 DEG C) separates from the top of liquid nitrogen storage tank 20, after cryogenic heat exchanger 18 heat exchange recovery section cold energy, and temperature Degree be increased to-150 DEG C, enter back in cryogenic heat exchanger 11 with compressed air heat exchange.And the liquid obtained bottom liquid nitrogen storage tank 20 Nitrogen then enters cryogenic heat exchanger 11 after flow valve 21, and flow is 72.2t/h, the cold energy needed for providing for air liquefaction.Change After heat, liquid nitrogen all gasifies, more blended valve 22 is mixed into circulating nitrogen gas with another strand of nitrogen flowed out from cryogenic heat exchanger 11 Stream, constitutes nitrogen and is about-59 DEG C for SAPMAC method, temperature.Meanwhile, the high pressure LNG flowed out from cryogenic heat exchanger 14 is the most complete Gasifying in portion, temperature is increased to-60.6 DEG C, pressure drop as little as 9.8MPa, becomes cryogenic high pressure natural gas flow, and flow is 120t/h.
(4) coolant media Rankine cycle
With circulating refrigerant medium 61t/h in the cryogenic high pressure natural gas flow entrance cryogenic heat exchanger 24 obtained in step (3) Tetrafluoroethane gas (temperature-9.4 DEG C, pressure 0.06MPa) heat exchange, all liquefies after tetrafluoroethane GAS ABSORPTION cold energy, becomes Tetrafluoroethane liquid.Pressure is entered low temperature after 0.04MPa is promoted to 0.31MPa through refrigerant pump 26 and changes by tetrafluoroethane liquid again With glycol water (20.0 DEG C, quality of glycol content the is 25%) heat exchange 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 supercharging is whole simultaneously Gasification, temperature is increased to-1.1 DEG C, then utilizes low temperature exhaust heat that tetrafluoroethane gas is heated to 25 DEG C in cryogenic heat exchanger 28, Subsequently into being expanded to 0.06MPa in coolant decompressor 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, may be used for Drive air compressor or nitrogen compressor, reduce 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-39.3 DEG C, and it is defeated Entering to utilize in cryogenic heat exchanger 25 sea water or other low temperature exhaust heat to be heated to more than 0 DEG C, pressure drop as little as 9.6MPa finally enters Gas distributing system.
(6) pressure-air cooling of LNG cold energy is utilized
The 221.6t/h obtained in step (4), the low-temperature glycol aqueous solution of 0 DEG C through glycol water pump 30 from After 0.15MPa is pressurized to 0.30MPa, then being divided into three strands through flow divider 31 and 32, one 84.3t/h sends in heat exchanger 5, one 69t/h sends into the interstage cooling in heat exchanger 7 for air compression process, also has one 68.3t/h to send in heat exchanger 9 and is used for Compressed-air actuated cooling.After heat exchange, the temperature of glycol water is increased to 20 DEG C, more blended valve 33 and 34 is mixed into one The hot glycol water of stock, then returns again to cryogenic heat exchanger 27, forms cold energy use circulation.During pressure-air cooling, There is portion of water to condense out, discharged by the condensate outlet of heat exchanger 5,7 and 9.
During whole air liquefaction, the cold energy utilizing the high pressure LNG gasification of 120t/h to discharge can produce 66.53t/h, The liquid air of 0.34MPa, total system power consumption is 8737kW (merit that deduction coolant media Rankine cycle produces), averagely produces 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, the one that therefore present invention proposes utilizes LNG cold energy to produce liquid air method and can save to produce liquid air The power consumption of 67.2%, utilizes the cold energy of 1 ton of LNG release can have good energy-saving effect with using electricity wisely 149kWh.
Above-described embodiment is the present invention preferably embodiment, but embodiments of the present invention are not by above-described embodiment Limit, the change made under other any spirit without departing from the present invention and principle, modify, substitute, combine, simplify, All should be the substitute mode of equivalence, within being included in protection scope of the present invention.

Claims (8)

1. one kind utilizes the method that cold energy of liquefied natural gas produces liquid air, it is characterised in that include operating in detail below step Rapid:
(1) air compression and purification
Air initially enters self-cleaning air intake filter device 1, removes dust contained in air and other in the filter After grain impurity, then mix with the non-liquefied air flowed out from cryogenic heat exchanger 11 in blender 3 after flow valve 2, then 0.5MPa it is compressed to step by step through air compressor 4,6 and 8；The compressed air discharged from air compressor 8 is cold through air cooler 9 But to slightly below room temperature, subsequently into air purifier 10 removes water, carbon dioxide and some Hydrocarbon in air, Become dry compressed air stream；
(2) air liquefaction
The dry compressed air stream obtained in step (1) enters in cryogenic heat exchanger 11, through with the liquid nitrogen flowed out from flow valve 21, Low temperature nitrogen in cryogenic heat exchanger 18, and the Cryogenic air heat exchange flowed out from liquid air storage tank 13；It is dried compression All liquefy after absorbed cold energy, then send in liquid air storage tank 13 after cryogenic throttle valve 12 blood pressure lowering；Empty from liquid The bottom of gas storage tank 13 obtains the liquid air product of desirable pressure, and the Cryogenic air that pressure reduction produces is then from liquid air The top of storage tank 13 is discharged, then mixes with raw air in return mixing valve 3 after cryogenic heat exchanger 11 reclaims cold energy；The opposing party Face, 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 liter Height, then in mixing valve 22, these two strands of nitrogen remix composition cyclic nitrogen air-flow；
(3) nitrogen is for SAPMAC method
The normal pressure liquefied natural gas (LNG) that need to vaporize is forced into 7～10MPa by LNG pump 23, becomes high pressure LNG, and temperature is- 145～-156 DEG C；The cyclic nitrogen air-flow obtained in step (2) in cryogenic heat exchanger 14 with high pressure LNG heat exchange, by circulating nitrogen gas Being cooled to-100 DEG C, then circulating nitrogen gas is compressed to high pressure by recycling nitrogen compressor 15,16 and 17 step by step；In order to reduce nitrogen The energy consumption of air compressor, circulating nitrogen gas all utilized high pressure LNG pre-cooling before entering nitrogen compressor in cryogenic heat exchanger 14 To-100 DEG C；From nitrogen compressor 17 cycle of higher pressure nitrogen out again cryogenic heat exchanger 14 with high pressure LNG heat exchange, temperature It is reduced to the high pressure LNG than entering cryogenic heat exchanger 14 high 2～5 DEG C；Cycle of higher pressure nitrogen after cooling is again through cryogenic heat exchanger 18 cool down further, then send into liquid nitrogen storage tank 20 after cryogenic throttle valve 19 blood pressure lowering；Reducing pressure by regulating flow produce low temperature nitrogen from The top of liquid nitrogen storage tank 20 separates, after cryogenic heat exchanger 18 heat exchange recovery section cold energy, enter back in cryogenic heat exchanger 11 with Compressed air heat exchange；The liquid nitrogen obtained bottom liquid nitrogen storage tank 20 then enters low-temperature heat exchange after flow valve 21 regulates flow Device 11, the cold energy needed for providing for air liquefaction；After heat exchange, liquid nitrogen all gasifies, more blended valve 22 with from cryogenic heat exchanger 11 Another strand of nitrogen flowed out is mixed into cyclic nitrogen air-flow, constitutes nitrogen for SAPMAC method；Meanwhile, flow from cryogenic heat exchanger 14 The high pressure LNG gone out the most all gasifies, and becomes cryogenic high pressure natural gas flow；
(4) coolant media Rankine cycle
With circulating refrigerant heat exchange, circulating refrigerant in the cryogenic high pressure natural gas flow entrance cryogenic heat exchanger 24 obtained in step (3) All liquefy after absorbing cold energy, become liquid coolant；Liquid coolant enters in cryogenic heat exchanger 27 after refrigerant pump 26 supercharging again With one hot glycol water heat exchange；After heat exchange, hot glycol water is cooled to 0～5 DEG C, becomes low-temperature glycol water Solution；Liquid coolant after supercharging the most all gasifies simultaneously, then utilizes sea water or low temperature exhaust heat by cold in cryogenic heat exchanger 28 Gas body is heated to more than 5 DEG C, and subsequently into expanding blood pressure lowering in coolant decompressor 29, the cold media gas after expansion returns again to low temperature Heat exchanger 24 liquefies, forms a coolant media Rankine cycle；The power of coolant media Rankine cycle output is used for driving sky Air compressor or nitrogen compressor, reduce 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 still below 0 DEG C, is inputted low temperature and changes Hot device 25 utilizes sea water or other low temperature exhaust heat are heated to more than 0 DEG C, finally enter gas distributing system；
(6) pressure-air cooling of LNG cold energy is utilized
The low-temperature glycol aqueous solution obtained in step (4) is after glycol water pump 30 supercharging, then through flow divider 31 and 32 It is divided into three strands, is respectively fed to the interstage cooling for air compression process in heat exchanger 5 and 7, and sends in air cooler 9 For compressed-air actuated cooling；After heat exchange, the temperature of glycol water is increased to 15～30 DEG C, more blended valve 33 and 34 mixes Synthesize one hot glycol water, then return again to cryogenic heat exchanger 27, form cold energy use circulation；Pressure-air cooling During, there is portion of water to condense out, discharged by the condensate outlet of heat exchanger 5,7 and 9.
The method utilizing cold energy of liquefied natural gas to produce liquid air the most according to claim 1, it is characterised in that: step (1) set up interstage cooler 5 and 7 between described air compressor 4,6 and 8, utilize low-temperature glycol aqueous solution to enter as low-temperature receiver Row interstage cooling.
The method utilizing cold energy of liquefied natural gas to produce liquid air the most according to claim 2, it is characterised in that: described Interstage cooler cools air to 5～10 DEG C.
The method utilizing cold energy of liquefied natural gas to produce liquid air the most according to claim 1, it is characterised in that: when returning When the non-liquefied air pressure returned is close to normal pressure, then before described in step (1), mixing valve 3 is placed in air compressor 4；Work as return Non-liquefied air pressure higher time, then after described in step (1), mixing valve 3 is placed in interstage cooler 5 or 7.
The method utilizing cold energy of liquefied natural gas to produce liquid air the most according to claim 1, it is characterised in that: step (3) circulating nitrogen gas described in is compressed to more than 6.0MPa step by step through nitrogen compressor 15,16 and 17.
The method utilizing cold energy of liquefied natural gas to produce liquid air the most according to claim 1, it is characterised in that: step (3) outlet pressure low compared with the outlet pressure of air compressor 8 0.02～0.11MPa of the cryogenic throttle valve 19 described in.
The method utilizing cold energy of liquefied natural gas to produce liquid air the most according to claim 1, 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.
The method utilizing cold energy of liquefied natural gas to produce liquid air the most according to claim 1, it is characterised in that: step (4) its output pressure of refrigerant pump 26 described in makes the bubble point temperature of coolant media at 0 DEG C.
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CN109595461A (en) * 2019-01-15 2019-04-09 江苏科技大学 A kind of LNG is regasified and liquid air preparation system and working method
CN109595461B (en) * 2019-01-15 2021-05-04 江苏科技大学 LNG regasification and liquid air preparation system and working method
WO2021043182A1 (en) * 2019-05-29 2021-03-11 苏州市兴鲁空分设备科技发展有限公司 Air separation apparatus and method using lng cold energy
CN110260148A (en) * 2019-06-28 2019-09-20 四川泰博流体科技有限公司 A kind of storage facilities of liquid air, method and air liquefying apparatus
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WO2021019143A1 (en) 2019-07-26 2021-02-04 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method for recovering refrigerating energy with electricity production or liquefying of a gaseous stream
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