WO2021043182A1 - 一种利用lng冷能的空分装置和方法 - Google Patents

一种利用lng冷能的空分装置和方法 Download PDF

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WO2021043182A1
WO2021043182A1 PCT/CN2020/113107 CN2020113107W WO2021043182A1 WO 2021043182 A1 WO2021043182 A1 WO 2021043182A1 CN 2020113107 W CN2020113107 W CN 2020113107W WO 2021043182 A1 WO2021043182 A1 WO 2021043182A1
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refrigerant
air
lng
cold energy
cold box
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PCT/CN2020/113107
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English (en)
French (fr)
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薛鲁
江楚标
贾盛兰
孙宁
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苏州市兴鲁空分设备科技发展有限公司
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Publication of WO2021043182A1 publication Critical patent/WO2021043182A1/zh

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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
    • 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
    • F25J3/0403—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 nitrogen
    • 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
    • F25J3/04018—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 main feed 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
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    • 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
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    • F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
    • F25J3/0406—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of nitrogen
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    • F25J3/04115—Arrangements of compressors and /or their drivers characterised by the type of prime driver, e.g. hot gas expander
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    • 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
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    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04218—Parallel arrangement of the main heat exchange line in cores having different functions, e.g. in low pressure and high pressure cores
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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
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    • 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
    • F25J3/04272—The cryogenic component does not participate in the fractionation and being liquefied hydrocarbons and comprising means for reducing the risk of pollution of hydrocarbons into the air fractionation
    • 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
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    • F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04351—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of 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
    • 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
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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
    • 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
    • F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
    • F25J3/04612—Heat exchange integration with process streams, e.g. from the air gas consuming unit
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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
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    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
    • F25J3/0489—Modularity and arrangement of parts of the air fractionation unit, in particular of the cold box, e.g. pre-fabrication, assembling and erection, dimensions, horizontal layout "plot"
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    • F25J2210/40—Air or oxygen enriched air, i.e. generally less than 30mol% of O2
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    • 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

Definitions

  • the invention belongs to the technical field of air separation, and specifically relates to an air separation device and method using LNG cold energy.
  • invention patent CN101943512B and other documents disclose air separation methods using the cold energy of liquefied natural gas. Although these methods use shallow cold NG to cool the intercooler of the air compressor as the raw material, the final cooler, the air compressor and the low-temperature nitrogen compressor oil. The ethylene glycol aqueous solution of the cooling liquid of the cooler and the motor realizes the cascade utilization of cold energy, but this cascade utilization efficiency is not high, and the compression heat of the raw material air compressor is wasted. Therefore, it is necessary to improve the existing air separation plant and method to increase the utilization rate of LNG cold energy.
  • the purpose of the present invention is to provide an air separation device that improves the utilization rate of LNG cold energy, thereby reduces the unit energy consumption of air separation products, saves equipment investment, and achieves better economic benefits and emission reduction benefits.
  • An air separation device using LNG cold energy including an air compression purification system that compresses and purifies raw air, a large cold box system that rectifies compressed and purified raw air to obtain air separation products, and is used to realize LNG
  • a small cold box system that exchanges heat with nitrogen that provides cold energy for the large cold box system
  • a refrigerant cycle system that uses natural gas cold energy from the small cold box system
  • a refrigerant cycle system that uses the refrigerant cycle system Coolant circulation system for natural gas cold energy.
  • the refrigerant circulation system includes a refrigerant liquefaction subcooler connected by a refrigerant circulation path, a refrigerant pressurizing pump, a raw material air cooler that exchanges heat with raw material air in the air compression and purification system, and Expansion generator set/refrigerant booster turboexpander, the natural gas exiting the small cold box system enters the refrigerant liquefaction subcooler to liquefy the refrigerant to subcool the refrigerant.
  • the raw material air cooler includes an intercooler and a final stage cooler.
  • the refrigerant liquefaction subcooler is arranged in the small cold box system or outside the small cold box system.
  • the coolant circulation system includes a coolant heat exchanger and a coolant circulation pump, and the natural gas and coolant exiting the refrigerant circulation system pass through the coolant heat exchanger.
  • the air compression and purification system includes a raw material air compressor, various raw material air coolers and an air purifier arranged in sequence.
  • the large cold box system includes a main heat exchanger and a rectification tower system arranged in sequence.
  • the small cold box system includes an LNG-nitrogen heat exchanger and a liquid nitrogen subcooler.
  • the nitrogen outlet pipe of the small cold box system is provided with an alarm interlocking hydrocarbon detector.
  • the low-temperature and low-pressure nitrogen output from the large cold box system is compressed to a specified pressure by a low-temperature and low-pressure nitrogen compressor or a refrigerant booster turbo-expansion unit, and then sent to the small cold box system.
  • the pressure nitrogen output from the system is also sent to the small cold box system.
  • the present invention also provides an air separation method using LNG cold energy used in the above-mentioned air separation device.
  • the air separation method is as follows: cascade use of the cold energy of LNG, first sending the LNG into a small cold box system to exchange heat with nitrogen, And use the liquid nitrogen obtained after heat exchange to rectify the raw material air to obtain air separation products to provide cold energy; and then send the natural gas out of the small cold box system into the refrigerant cycle system to exchange heat with the refrigerant, and use the After being heated, the subcooled refrigerant is liquefied to cool the compressed air, and the refrigerant, which is vaporized and heated by the air, expands the generator set or the refrigerant booster turboexpander set to expand and perform work; finally, the refrigerant is discharged The natural gas with part of the cooling capacity of the circulation system is sent to the coolant circulation system to exchange heat with the coolant, and the coolant after the heat exchange is used to cool the equipment that needs to be cooled.
  • the present invention has the following advantages compared with the prior art: the present invention can make the cold energy of liquefied natural gas better cascade utilization, and also use the waste heat of the compressor to make liquid air separation products The unit energy consumption has been further reduced, which can save equipment investment and achieve better economic and emission reduction benefits.
  • Figure 1 is a schematic diagram of the process flow of the first embodiment of the present invention.
  • Figure 2 is a schematic diagram of the process flow of the second embodiment of the present invention.
  • Fig. 3 is a schematic diagram of the process flow of the third embodiment of the present invention.
  • Fig. 4 is a schematic diagram of the process flow of the fourth embodiment of the present invention.
  • Embodiment 1 An air separation plant using LNG cold energy capable of generating electricity at the same time, including an air compression purification system A, a large cold box system B, a small cold box system C, a refrigerant circulation system D, and a coolant circulation system E.
  • the air compression and purification system A is used to compress and purify the raw material air, and it includes a raw material air compressor 1, a raw material air cooler 2 and an air purifier 3 arranged in sequence.
  • the raw material air cooler 2 includes an intercooler and a final stage cooler.
  • the raw material air cooler 2 uses a refrigerant as a refrigerant.
  • the large cold box system B is used to rectify the compressed and purified raw air 102 to obtain air separation products, and the large cold box system B uses liquid nitrogen to provide the required cold energy.
  • the large cold box system B includes a main heat exchanger 5 and a rectification column system arranged in sequence, while the rectification column system includes an upper column 8, a lower column 10, a main condensing evaporator 9, a nitrogen liquefier 6 and/or oxygen liquefaction
  • the vessel 14, the liquid nitrogen and liquid separators 7, 11, the liquid nitrogen subcooler 12 and the liquid air liquid oxygen subcooler 13, may also include an argon production system.
  • the supercooling system of liquid air, liquid nitrogen, and liquid oxygen in the large cold box system B can be organized arbitrarily, and can be combined to supercool, or another organization can be supercooled.
  • the small cold box system C is used to realize heat exchange between LNG and nitrogen that provides cold energy for the large cold box system.
  • the small cold box system includes an LNG-nitrogen heat exchanger 18 and a liquid nitrogen subcooler 19.
  • the nitrogen outlet pipe of the small cold box system C can also be equipped with an alarm interlocking hydrocarbon detector to ensure the safety of the device.
  • the refrigerant circulation system D is used to utilize the cold energy of natural gas from the small cold box system C. It includes a refrigerant liquefaction subcooler 21 connected by a refrigerant circulation path, a refrigerant pressurizing pump 23, a raw material air cooler 2 that exchanges heat with raw air in the air compression and purification system A, and an expansion generator set 22.
  • the natural gas of the small cold box system C enters the refrigerant liquefaction subcooler 21 and exchanges heat with the refrigerant 401, so that the refrigerant 401 is liquefied and supercooled.
  • the refrigerant can be R22, R134a, R143a or other refrigerants with similar physical properties.
  • the refrigerant liquefaction subcooler 21 can be installed in the small cold box system C or outside the small cold box system C.
  • the refrigerant circulation system E is used to utilize the cold energy of natural gas from the refrigerant circulation system D. It includes a coolant heat exchanger 27 and a coolant circulation pump 26. The natural gas and the coolant 501 out of the refrigerant circulation system D pass through the coolant heat exchanger 27 and exchange heat.
  • the coolant is an aqueous glycol solution.
  • the raw material air is sucked in through the air filter, and first enters the raw material air compressor 1 to compress to about 0.5Mpa.
  • the compressed raw material air 101 exchanges heat in the raw material air cooler 2 and then goes to the purifier 3 to remove carbon dioxide, water, acetylene, etc. Impurities, the compressed and purified raw air 102 is obtained.
  • the purifier 3 uses the waste nitrogen from the large cold box to heat, regenerate and blow cool, and then vent the waste nitrogen.
  • the purified compressed raw air 102 exchanges heat with the reflux gas in the main heat exchanger 5 and is cooled to a predetermined temperature, and then is sent to the lower tower 10.
  • an oxygen-rich liquid air 103 is obtained at the bottom, and pressure nitrogen is obtained at the top.
  • a part of the pressure nitrogen 104 is drawn into the nitrogen liquefier 6 to exchange heat and liquefy with the throttling liquid nitrogen 206 from the small cold box, and then return to the top of the lower tower 10 to realize the transfer of cold energy.
  • the remaining pressure nitrogen enters the main condensing evaporator 9, where it is condensed into liquid nitrogen by the liquid oxygen at the bottom of the upper tower 8.
  • a part of the liquid nitrogen is sent back to the top of the lower tower to maintain the distillation conditions of the lower tower, and the other part of the liquid nitrogen 111 is subcooled by the liquid nitrogen subcooler 12 and most of the throttling is sent to the top of the upper tower 8 to participate in the rectification. Part of it is sent to the gas-liquid separator 11 as a liquid nitrogen product.
  • the throttling liquid nitrogen 206 from the small cold box system C is liquefied in the nitrogen liquefier 6 and the excess part 207 after the pressure nitrogen 104 is subcooled by the liquid nitrogen subcooler 12 and then sent to the gas-liquid separator 11 as a liquid nitrogen product.
  • the pressure nitrogen 109 of the gas-liquid separator 7 and the nitrogen liquefier 6 is reheated in the main heat exchanger 5 and then exits the large cold box system B, and merges with the pressure nitrogen of the low-temperature and low-pressure nitrogen compressor 15.
  • the oxygen-rich liquid air 103 exiting the lower tower is subcooled by the liquid-air liquid oxygen subcooler 13 and then throttling and sending it to the middle of the upper tower 8 to participate in rectification.
  • Most of the liquid nitrogen 111 sent to the upper tower 8, the oxygen-enriched liquid space 103 and the gas oxygen evaporated by the main condensing evaporator 9 are rectified again, and low pressure nitrogen 107 is obtained from the top of the upper tower 8, and polluted from the upper portion of the upper tower 8.
  • Nitrogen 106 the argon fraction is obtained from the middle of the upper column 8, and liquid oxygen is obtained at the bottom of the upper column 8.
  • Part of the liquid oxygen exchanges heat with the nitrogen from the top of the lower column 10 in the main condensing evaporator 9 to liquefy the nitrogen into liquid nitrogen, liquid oxygen After being transformed into oxygen, it participates in the rectification of the upper tower.
  • Part of the liquid oxygen 105 is extracted from the bottom of the upper tower, and is led out as a product after being supercooled by the liquid-air liquid oxygen subcooler 13.
  • the sewage nitrogen 106 obtained from the upper part of the upper tower 8 is reheated in the liquid nitrogen subcooler 12, the liquid air liquid oxygen subcooler 13 and the main heat exchanger 5, and then goes to the air purifier 3 as regeneration gas. Or empty.
  • the argon fraction extracted from the middle of the upper column 8 is then sent to the argon production system to produce product liquid argon, which is well known to those skilled in the art and will not be described in detail here.
  • the low pressure nitrogen 107 obtained from the top of the upper tower 8 is reheated in the liquid nitrogen subcooler 12, the liquid air liquid oxygen subcooler 13 and the main heat exchanger 5.
  • a part of the low pressure nitrogen is used as the product GN2 to lead out the large cold box system B, and the other A part of the low-pressure nitrogen 110 is extracted from the set temperature position in the middle of the main heat exchanger 5.
  • This part of low-temperature and low-pressure nitrogen 110 is sent out of cold box system B and then sent to low-temperature and low-pressure nitrogen compressor 15 to be compressed to a specified pressure. After coming out of low-temperature and low-pressure nitrogen compressor 15, it merges with pressure nitrogen 109 from cold box system B to form nitrogen 201 Then it is sent to the small cold box system C.
  • Nitrogen 201 enters the LNG-nitrogen heat exchanger 18 for multiple cycles for heat exchange. First, it is cooled to -100°C ⁇ -150°C in the LNG-nitrogen heat exchanger 18 and then merged with the reflux pressure nitrogen 202 heated to the same temperature, and then sent to the low temperature medium pressure nitrogen compressor section 16 to be compressed into pressure nitrogen. 203.
  • the pressure nitrogen 203 enters the LNG-nitrogen heat exchanger 18 and is cooled to -100°C ⁇ -150°C, and then merges with the reflux pressure nitrogen 204 heated to the same temperature and enters the second stage 17 of the low temperature and medium pressure nitrogen compressor unit. After compression, the high-pressure nitrogen gas 205 is formed.
  • the high-pressure nitrogen gas 205 enters the LNG-nitrogen heat exchanger 18 to exchange heat and liquefy with the LNG pressurized to a specified pressure and the two reflux nitrogen gas 202 and 204, and then enters the liquid nitrogen subcooler. In 19, it is further subcooled by two reflux nitrogen 202 and 204, and then divided into three channels, one is throttling into reflux 202, the other is reflux 204, and the other 206 is sent to large cold box system B, which is large cold box system B. Provide cold energy and transfer the cold energy to the rectification system for air separation.
  • the LNG that enters the LNG-nitrogen heat exchanger 18 is divided into two paths.
  • One path 301 is reheated to above 0°C to the pipe network, and the other path has a certain amount of cold energy shallow cooling NG302 enters the refrigerant cycle system D to liquefy and supercool the refrigerant
  • the device 21 exchanges heat with the refrigerant 401 therein to liquefy and supercool it.
  • the supercooled refrigerant is pressurized to a predetermined pressure by the refrigerant pressure pump 23 and then sent to the intercooler and the end of the raw material air cooler 2
  • the stage cooler cools the raw air, and the refrigerant 401 after gasification and temperature rises to expand the generator set 22 to expand, reduce pressure and reduce temperature, and drive the generator to generate electricity, and the refrigerant circulates.
  • the intercooler can be one or two
  • the final cooler can be combined to form a heat exchanger to exchange heat with the refrigerant, or they can be set separately to form 2 to 3 heat exchangers to exchange heat with the refrigerant. Exchange the heat, and then combine 2 to 3 refrigerants into 401 before entering the expansion generator set 22.
  • the NG302 out of the refrigerant liquefaction subcooler 21 still has some cold energy, and then it is sent to the coolant heat exchanger 27 (ie, glycol water solution heat exchanger) to exchange heat with the coolant 501 (ie, glycol water solution) for cooling.
  • Coolant 501 cools down, and the cooled coolant 501 is sent to raw material air compressors, low-temperature nitrogen compressors, oil coolers and motor coolers of expansion generator sets as a coolant, and the heated coolant 501 passes through the coolant circulation pump 26 (ie, ethylene glycol aqueous solution pump) realizes circulation after pressurizing.
  • the NG302 that exits the coolant heat exchanger 27 has reached above 0°C, and it merges with 301 and then is sent to the receiving station NG output pipe network.
  • the low-temperature and low-pressure nitrogen compressor 15 can also be dispensed with. At this time, the liquid nitrogen output of the device will be reduced, and the low-temperature and low-pressure nitrogen 110 can be eliminated accordingly.
  • the air separation method using LNG cold energy used in the above air separation plant is: cascade use of LNG cold energy, first send the LNG into the small cold box system C to exchange heat with nitrogen, and use the heat exchange to obtain The liquid nitrogen is used to rectify the raw air to obtain the air separation product to provide cold energy; then the natural gas from the small cold box system C is sent to the refrigerant cycle system D to exchange heat with the refrigerant, and the heat exchange has been liquefied and supercooled The refrigerant cools the compressed air (the liquefied and subcooled refrigerant exchanges heat with the compressed air), and the waste heat after the air is compressed by the gasified and heated refrigerant expands the generator set 22 to perform work expansion and provide kinetic energy; Finally, the natural gas with part of the cooling capacity from the refrigerant circulation system D is sent to the refrigerant circulation system E to exchange heat with the coolant, and the heat exchanged coolant is used to cool the equipment to be cooled.
  • Embodiment 2 As shown in Figure 2, an air separation method and device using LNG cold energy that can generate electricity at the same time.
  • the upper tower 8 mainly produces gas and oxygen 112 instead of producing gas.
  • Liquid oxygen 105 Part of the liquid nitrogen 206 throttling from the small cold box system C in the deoxygenation liquefier 14 is liquefied and supercooled the gaseous oxygen 112 drawn from the bottom of the upper tower to turn it into a liquid oxygen product.
  • the low-temperature and low-pressure nitrogen compressor 15 can also be dispensed with. At this time, the liquid nitrogen output of the device will be reduced, and the low-temperature and low-pressure nitrogen 110 can also be eliminated accordingly.
  • Embodiment 3 As shown in Figure 3, an air separation method and device using LNG cold energy that can simultaneously pressurize low-temperature and low-pressure nitrogen to the pressure required by the process.
  • the main difference from the first embodiment is: low-temperature and low-pressure nitrogen
  • the 110 uses a refrigerant booster turboexpander unit, that is, the booster ends of two parallel refrigerant booster turboexpanders 24 and 25 are compressed in series to reach the process pressure.
  • the expansion ends of the refrigerant supercharging turbine expansion units 24 and 25 are connected in parallel, and the supercharging ends are connected in series.
  • the refrigerant 401 exiting the heat exchanger 2 is divided into three paths: one way to the supercharger turbine expander 24, the other way to the supercharger turbine expander 25, and the remaining refrigerant is throttled to the supercharger turbine expander 24. , 25
  • the refrigerant at the outlet of the expansion end merges and goes to the refrigerant liquefaction subcooler 21. If there is a lot of excess refrigerant, an expansion unit can also be installed to generate electricity.
  • the natural gas from the small cold box system C is sent to the refrigerant liquefaction subcooler 21 to exchange heat with the refrigerant to make it liquefied and supercooled.
  • the liquefied and supercooled refrigerant exchanges heat with the compressed air and absorbs the waste heat of the air.
  • the refrigerant provides kinetic energy for the refrigerant booster turboexpander units 24 and 25.
  • the liquid nitrogen 206 from the small cold box system C is throttled again by a part of the deoxygenating liquefier 14, where it is liquefied and subcooled the gaseous oxygen 112 drawn from the bottom of the upper tower 8 to make it liquid Oxygen products.
  • a refrigerant booster turbo expander 24 may be used to pressurize the low-temperature and low-pressure nitrogen to the process requirements, so that one refrigeration unit can be reduced. ⁇ pressurized turboexpander 25.
  • the present invention is not limited to the above-mentioned specific embodiments.
  • the above-mentioned specific embodiments are only illustrative and not restrictive, whether it is a liquid air separation device or an internal compression process air separation device that produces partial liquid products at the same time.
  • Device as long as the shallow cold NG from the LNG-nitrogen heat exchanger is used to liquefy the supercooled refrigerant and use the compressed waste heat of the compressor to generate electricity through the expansion unit or pressurize the low-pressure low-temperature nitrogen to the pressure required by the process to replace the low-pressure
  • the low-temperature nitrogen compressor falls within the protection scope of the present invention.
  • the present invention provides two basic implementation schemes, both of which use the liquid nitrogen produced in the small cold box system C to provide the large cold box system B with cold energy and part of the liquid nitrogen products.
  • the first solution uses two turboexpanders 24 and 25 that use refrigerants as working fluids.
  • the low-temperature and low-pressure nitrogen is pressurized to the pressure required by the process through the series pressurization of the pressurizing end to replace the original low temperature.
  • Low pressure nitrogen compressor Low pressure nitrogen compressor.
  • the second set of plans uses a refrigerant expansion generator set to generate electricity for its own use.
  • the core of the above solution is the use of refrigerant as the intercooler of the raw material air cooler 2 after the raw material air compressor 1, and the cooling liquid of the final cooler.
  • the refrigerant absorbs the compressed waste heat of the compressed air and then vaporizes and heats up, and then goes through
  • the flat expander generator set 22 generates power or the refrigerant supercharged turboexpander sets 24, 25 pressurize the low-temperature and low-pressure nitrogen gas to meet the process requirements.
  • the liquid nitrogen that is sent to the large cold box system B obtained from the LNG heat exchanger is depressurized and with whom to exchange heat (the bottom gas nitrogen out of the tower, the gas oxygen out of the upper tower bottom, and the Cold box air, etc.), no matter what the NG residual cold of the refrigerant liquefier 21 is used for, or whether it is necessary to produce high-purity liquid oxygen, internally compressed oxygen and nitrogen products, etc., as long as the above are used, the raw material air pressure can be satisfied.
  • the present invention develops the cascade utilization technology of LNG cold energy, and ingeniously combines the shallow cold energy of LNG in the cold energy air separation with the compressed waste heat of the raw material air compressor
  • the organization uses it to form a power generation cycle for self-use or uses a refrigerant booster turbo expander to pressurize low-temperature and low-pressure nitrogen to replace the original low-temperature and low-pressure nitrogen compressor.
  • both power generation and self-use or low-temperature and low-pressure nitrogen pressure In order to replace the original low-temperature and low-pressure nitrogen compressor, it does not change the inlet temperature of the second and third stages of the air compressor and the exhaust temperature of the final stage outlet, nor does it change the compressor oil cooler and the coolant and cooling temperature of the motor.
  • the cold energy of LNG is used more effectively, and the waste heat of compressed air is also used, so that the unit power consumption of liquid air separation products is significantly reduced, and the CO 2 emission reduction is also significantly increased, which can achieve better Economic and social benefits.
  • the unit power consumption of liquid air separation products can be reduced by about 7% on the original basis, and the CO 2 emission reduction can be increased by about 7%, which effectively increases the utilization efficiency of LNG cold energy and further reduces the liquid The cost of air separation products and equipment investment.
  • the unit power consumption of the liquid air separation product of the air separation plant using the cold energy of liquefied natural gas of the present invention can be reduced from the original 0.36KWh/Nm 3 to about 0.33Wh/Nm 3 , which is the most advanced About 41% of the conventional process, and does not consume refrigerant water, it is an effective measure for the development of circular economy, energy saving and emission reduction, and has obvious social and economic benefits.

Abstract

本发明涉及一种利用LNG冷能的空分装置和方法。利用LNG冷能的空分装置包括对原料空气进行压缩和净化的空气压缩净化系统、对压缩净化后的原料空气进行精馏而获取空分产品的大冷箱系统、用于实现LNG与为大冷箱系统提供冷能的氮之间换热的小冷箱系统、利用出小冷箱系统的天然气冷能的制冷剂循环系统、利用出制冷剂循环系统的天然气冷能的冷却剂循环系统。利用LNG冷能的空分方法将LNG的冷能先后用于精馏原料空气、与制冷剂换热及与冷却剂换热。本发明实现了液化天然气的冷能最充分的梯级利用，使液体空分产品的单位能耗得到了进一步降低，可节省设备投资，取得更好的经济效益和减排效益。

Description

一种利用LNG冷能的空分装置和方法 技术领域
本发明属于空分技术领域，具体涉及一种利用LNG冷能的空分装置和方法。
背景技术
现有技术中，常利用LNG来为空分装置提供冷能，但目前存在对LNG冷能的梯级利用不充分的问题。例如发明专利CN101943512B等文献公开的利用液化天然气冷能的空气分离方法，这些方法虽然用浅冷NG来冷却作为原料空压机中间冷却器、末级冷却器及空压机和低温氮压机油冷却器与电机的冷却液的乙二醇水溶液，实现了冷能的梯级利用，但这种梯级利用效率不高，原料空压机的压缩热也白白浪费了。因此，有必要改进现有的空分装置和方法来提高LNG冷能的利用率。
发明内容
本发明的目的是提供一种提高LNG冷能利用率，从而降低空分产品的单位能耗、节省设备投资，取得更好的经济效益和减排效益的空分装置。
为达到上述目的，本发明采用的技术方案是：
一种利用LNG冷能的空分装置，包括对原料空气进行压缩和净化的空气压缩净化系统、对压缩净化后的原料空气进行精馏而获取空分产品的大冷箱系统、用于实现LNG与为所述大冷箱系统提供冷能的氮之间换热的小冷箱系统、利用出所述小冷箱系统的天然气冷能的制冷剂循环系统、利用出所述制冷剂循环系统的天然气冷能的冷却剂循环系统。
优选的，所述制冷剂循环系统包括通过制冷剂循环通路相连接的制冷剂液化过冷器、制冷剂加压泵、与所述空气压缩净化系统中的原料空气换热的原料空气冷却器以及膨胀发电机组/制冷剂增压透平膨胀机组，所述出所述小冷箱系统的天然气进入所述制冷剂液化过冷器使制冷剂液化过冷。
所述原料空气冷却器包括中间冷却器和末级冷却器。
所述制冷剂液化过冷器设置在所述小冷箱系统内，或设置在所述小冷箱系统外。
优选的，所述冷却剂循环系统包括冷却剂换热器及冷却剂循环泵，出所述制冷剂循环系统的天然气和冷却剂均通过所述冷却剂换热器。
优选的，所述空气压缩净化系统包括依次设置的原料空压机、各级原料空气冷却器和空气纯化器。
优选的，所述大冷箱系统包括依次设置的主换热器和精馏塔系统。
优选的，所述小冷箱系统包括LNG-氮换热器和液氮过冷器。
优选的，所述小冷箱系统的氮出口管上设置有报警联锁的碳氢化合物检测仪。
优选的，由所述大冷箱系统输出的低温低压氮气经低温低压氮压机或制冷剂增压透平膨胀机组压缩到规定压力后送入所述小冷箱系统，由所述大冷箱系统输出的压力氮气也送入所述小冷箱系统。
本发明还提供一种上述空分装置采用的利用LNG冷能的空分方法，所述空分方法为：梯级利用LNG的冷能，先将LNG送入小冷箱系统中与氮换热，并利用换热后得到的液氮为精馏原料空气而获得空分产品提供冷能；再将出所述小冷箱系统的天然气送入制冷剂循环系统中与制冷剂换热，并利用换热后已液化过冷的制冷剂去冷却压缩后的空气，被空气气化升温后的所述制冷剂去膨胀发电机组或制冷剂增压透平膨胀机组膨胀做功；最后将出所述制冷剂循环系统的还带有部分冷量的天然气送入冷却剂循环系统中与冷却剂换热，并利用换热后的冷却剂来冷却需冷却的设备。
由于上述技术方案运用，本发明与现有技术相比具有下列优点：本发明能够使液化天然气的冷能得到更好的梯级利用，并将压缩机的废热也利用了起来，使液体空分产品的单位能耗得到了进一步降低，可节省设备投资，取得更好的经济效益和减排效益。
附图说明
附图1为本发明的实施例一的工艺流程示意图。
附图2为本发明的实施例二的工艺流程示意图。
附图3为本发明的实施例三的工艺流程示意图。
附图4为本发明的实施例四的工艺流程示意图。
具体实施方式
下面结合附图所示的实施例对本发明作进一步描述。
实施例一：一种可同时发电的利用LNG冷能的空分装置，包括空气压缩净化系统A、大冷箱系统B、小冷箱系统C、制冷剂循环系统D和冷却剂循环系统E。
空气压缩净化系统A用于对原料空气进行压缩和净化，其包括依次设置的原料空压机1、各级原料空气冷却器2和空气纯化器3。原料空气冷却器2包括中间冷却器和末级冷却器。原料空气冷却器2中用制冷剂作冷媒。
大冷箱系统B用于对压缩净化后的原料空气102进行精馏而获取空分产品，大冷箱系统B利用液氮提供所需冷能。大冷箱系统B包括依次设置的主换热器5和精馏塔系统，而精馏塔系统则包括上塔8、下塔10、主冷凝蒸发器9、氮液化器6和/或氧液化器14、液氮气液分离器7、11以及液氮过冷器12和液空液氧过冷器13，还可以包括制氩系统。大冷箱系统B内液空、液氮、液氧的过冷系统是可以任意组织的，可以合在一起过冷，也可以另 外组织过冷。
小冷箱系统C用于实现LNG与为大冷箱系统提供冷能的氮之间换热。小冷箱系统包括LNG-氮换热器18和液氮过冷器19。在小冷箱系统C的氮出口管上还可以设置报警联锁的碳氢化合物检测仪以确保装置的安全。
制冷剂循环系统D用来利用出小冷箱系统C的天然气的冷能。它包括通过制冷剂循环通路相连接的制冷剂液化过冷器21、制冷剂加压泵23、与空气压缩净化系统A中的原料空气换热的原料空气冷却器2以及膨胀发电机组22，出小冷箱系统C的天然气进入制冷剂液化过冷器21与制冷剂401换热，使制冷剂401液化过冷。制冷剂可以是R22，也可以是R134a，R143a或物性类似的其它制冷剂。为节省占地，方便配管和便于保温，制冷剂液化过冷器21可以设置在小冷箱系统C内或小冷箱系统C外。
冷却剂循环系统E用来利用出制冷剂循环系统D的天然气的冷能。它包括冷却剂换热器27和却剂循环泵26，出制冷剂循环系统D的天然气和冷却剂501均通过冷却剂换热器27并进行换热。本实施例中，冷却剂为乙二醇水溶液。
原料空气经空气过滤器吸入，先进入原料空压机1中压缩达到0.5Mpa左右，压缩后的原料空气101在原料空气冷却器2中换热降温后去纯化器3除去二氧化碳、水、乙炔等杂质，得到压缩净化后的原料空气102。纯化器3用大冷箱来的废氮加热再生吹冷，然后废氮放空。
净化后的压缩原料空气102在主换热器5中与返流气体换热降温到规定温度后送入下塔10。空气在下塔10经初步分离后，在底部得到富氧液空103，在顶部得到压力氮气。抽出一部分压力氮气104进入氮气液化器6中与从小冷箱来的节流后液氮206换热液化后返回下塔10的顶部，实现冷量的传递。其余压力氮气进入主冷凝蒸发器9，在其中被上塔8底部的液氧冷凝成液氮。该液氮的一部分送回下塔顶以维持下塔的精馏工况，另一部分液氮111经液氮过冷器12过冷后大部分节流送入上塔8顶部参与精馏，少部分送入气液分离器11作为液氮产品。从小冷箱系统C来的节流后液氮206在氮液化器6中液化压力氮气104后的多余部分207经液氮过冷器12过冷后送入气液分离器11作为液氮产品。出气液分离器7及氮气液化器6的压力氮气109在主换热器5复热后出大冷箱系统B，与出低温低压氮压机15的压力氮气汇合。出下塔的富氧液空103经液空液氧过冷器13过冷后节流送入上塔8中部参与精馏。送入上塔8的液氮111的大部分、富氧液空103与主冷凝蒸发器9蒸发的气氧进行再次精馏，从上塔8顶部得到低压氮气107，从上塔8上部得到污氮气106，从上塔8中部得到氩馏分，在上塔8底部得到液氧，部分液氧在主冷凝蒸发器9与从下塔10顶部来的氮气换热使氮气液化成为液氮，液氧气化成氧气后参与上塔的精馏，部分液氧105从上塔底部抽出，经液空液氧过冷器13过冷后作为产品引出。从上塔8上部得到的污氮气106在 液氮过冷器12，液空液氧过冷器13及主换热器5中复热出大冷箱系统B后去空气纯化器3作为再生气或放空。从上塔8中部抽出的氩馏分则送入制氩系统制取产品液氩，该制氩系统是本行业技术人员所熟知的，在此不再细述。
从上塔8顶部得到的低压氮气107在液氮过冷器12，液空液氧过冷器13及主换热器5中复热，一部分低压氮气作为产品GN2引出大冷箱系统B，另一部分低压氮气110从主换热器5中部设定温度位置抽出。这部分低温低压氮气110出大冷箱系统B后送入低温低压氮压机15压缩到规定压力，出低温低压氮压机15后与从大冷箱系统B出来的压力氮109汇合成氮气201后送入小冷箱系统C。
氮气201进入LNG-氮换热器18中多次循环进行换热。首先其在LNG-氮换热器18中被冷却到-100℃～-150℃后与升温到相同温度的返流压力氮气202汇合后送入低温中压氮气压缩机一段16被压缩成压力氮气203，压力氮气203再进入LNG-氮换热器18冷却到-100℃～-150℃后，再与升温到相同温度的返流压力氮气204汇合后进入低温中压氮气压缩机组的二段17进行压缩，压缩后形成高压氮气205，高压氮气205进入LNG-氮换热器18与加压到规定压力的LNG及两股返流氮气202和204换热液化后，再进入液氮过冷器19中被两股返流氮气202、204进一步过冷后分成三路，一路经再节流成返流202，一路即返流204，一路206送大冷箱系统B而为大冷箱系统B提供冷能，将冷量传递给用于空分的精馏系统。
进LNG-氮换热器18的LNG分成两路，一路301复热到0℃以上去管网，另一路还有一定冷能的浅冷NG302进入制冷剂循环系统D中的制冷剂液化过冷器21，与其中的制冷剂401换热而使其液化并过冷，过冷后的制冷剂经制冷剂加压泵23加压到规定压力后送原料空气冷却器2的中间冷却器和末级冷却器去冷却原料空气，气化升温后的制冷剂401再去膨胀发电机组22膨胀降压降温并带动发电机发电，制冷剂则实现循环。中间冷却器(可以是一个，也可以是两个)和末级冷却器可以合在一起组成一个换热器与制冷剂换热，也可以分开设置组成2到3个换热器分别与制冷剂换热，然后再将2到3股制冷剂汇合成401后再进膨胀发电机组22。
出制冷剂液化过冷器21的NG302还有一些冷能，再送入冷却剂换热器27(即乙二醇水溶液换热器)与冷却剂501(即乙二醇水溶液)进行换热使冷却剂501降温，降温后的冷却剂501送原料空压机、低温氮压机和膨胀发电机组的油冷却器及电机冷却器等设备处作为冷却剂，升温后的冷却剂501经冷却剂循环泵26(即乙二醇水溶液泵)增压后实现循环。出冷却剂换热器27的NG302已达0℃以上，与301汇合后送接收站NG输出管网。
低温低压氮压机15也可以不用，这时装置的液氮产量将减少，低温低压氮气110这一路也可相应取消。
由以上方案可知，上述空分装置采用的利用LNG冷能的空分方法为：梯级利用LNG的冷能，先将LNG送入小冷箱系统C中与氮换热，并利用换热后得到的液氮为精馏原料空气而获得空分产品提供冷能；再将出小冷箱系统C的天然气送入制冷剂循环系统D中与制冷剂换热，并利用换热后已液化过冷的制冷剂冷却压缩后的空气(液化过冷后的制冷剂与压缩后的空气进行换热)，被空气压缩后的废热气化升温后的制冷剂去膨胀发电机组22膨胀做功，提供动能；最后将出制冷剂循环系统D的还带有部分冷量的天然气送入冷却剂循环系统E中与冷却剂换热，并利用换热后的冷却剂来冷却需冷却的设备。
实施例二：如附图2所示，一种可同时发电的利用LNG冷能的空分方法和装置，其与实施例一的主要不同是：上塔8主要是产气氧112而不是产液氧105。从小冷箱系统C来的液氮206节流后的一部分去氧液化器14液化并过冷从上塔底部引出的气氧112，使其成为液氧产品。
其中的低温低压氮压机15也可以不用，这时装置的液氮产量将减少，低温低压氮气110这一路也可相应取消。
实施例三：如附图3所示，一种可同时将低温低压氮气增压到工艺要求压力的利用LNG冷能的空分方法和装置，其与实施例一的主要不同是：低温低压氮气110是用制冷剂增压透平膨胀机组，即两台并连的制冷剂增压透平膨胀机24、25的增压端串联压缩使其达到工艺要求压力的。冷剂增压透平膨胀机组24、25的膨胀端是并联的，增压端是串联的。出换热器2的制冷剂401被分成三路：一路去增压透平膨胀机24，一路去增压透平膨胀机25，其余的制冷剂经节流后与增压透平膨胀机24、25膨胀端出口的制冷剂汇合后去制冷剂液化过冷器21。如多余的制冷剂较多，也可再设一膨胀机组发电。出小冷箱系统C的天然气送入制冷剂液化过冷器21中与制冷剂换热而使其液化过冷，液化过冷后的制冷剂与压缩后的空气换热，吸收空气废热后的制冷剂为制冷剂增压透平膨胀机组24、25提供动能。在该实施例中，从小冷箱系统C来的液氮206经再次节流后的一部分去氧液化器14，在其中液化并过冷从上塔8底部引出的气氧112，使其成为液氧产品。
若膨胀机的增压端可以实现用两个叶轮串联增压，这时用一台制冷剂增压透平膨胀机24就可能使低温低压氮气增压到工艺要求，这样就可以减少一台制冷剂增压透平膨胀机25。
实施例四：如附图4所示，一种可同时将低温低压氮气增压到工艺要求压力的利用LNG冷能的空分方法和装置，其与实施例三的主要不同是：既使用了氮液化器6，又使用了氧液化器14。
应该指出，本发明不局限于上述的具体实施方式，上述的具体实施方式仅仅是示意性的，并不是限制性的，无论是液体空分装置，还是同时生产部分液体产品的内压缩流程空分 装置，只要将出LNG-氮换热器的浅冷NG用来液化过冷制冷剂并将压缩机的压缩废热利用起来通过膨胀机组发电或使低压低温氮气增压到工艺要求的压力以取代低压低温氮压机，则均属于本发明的保护范围之内。
由以上各实施例可知，本发明提供了两套基本实施方案，两套方案都用小冷箱系统C内生产的液氮为大冷箱系统B提供冷能和部分液氮产品。第一套方案使用了以制冷剂为工质的两台增压透平膨胀机24、25，通过增压端的串联增压使低温低压氮气增压到工艺所要求的压力，以取代原来的低温低压氮压机。第二套方案则使用了制冷剂膨胀发电机组发电自用。上述方案的核心在用制冷剂作为原料空压机1之后的原料空气冷却器2的中间冷却器、末级冷却器的冷却液，制冷剂吸收压缩空气的压缩废热后气化升温，然后去透平膨胀机发电机组22发电或冷剂增压透平膨胀机组24、25增压低温低压氮气到满足工艺要求。无论冷能空分的其余部分流程如何组织，由LNG换热器得到的送大冷箱系统B的液氮降压后与谁换热(出下塔顶气氮，出上塔底气氧，进冷箱空气等)，也无论出制冷剂液化器21的NG余冷作何利用，也无论要不要同时生产高纯液氧、内压缩氧氮产品等，只要使用了以上既能满足原料空压机中间冷却器、末级冷却器的冷却需要，又利用了原料空压机1的压缩废热使之发电或使低温低压氮气增压到工艺要求的某种冷剂，就都是使用了本专利的核心技术。
本发明在现有利用LNG冷能的空分流程和装置的基础上，发展了LNG冷能的梯级利用技术，将冷能空分中LNG的浅冷冷能与原料空压机的压缩废热巧妙的组织利用起来组成发电循环发电自用或采用冷剂增压透平膨胀机增压低温低压氮气以取代原来的低温低压氮压机，通过制冷剂循环既实现了发电自用或使低温低压氮气增压以取代原来的低温低压氮压机，又不改变空压机二、三级的进气温度和末级出口的排气温度，也不改变压缩机油冷却器及电机的冷却液和冷却温度，使LNG冷能得到了更有效的利用，并将压缩空气的废热也利用了起来，从而使液体空分产品的单位电耗有明显降低，CO 2减排量也明显增加，可取得更好的经济效益和社会效益。经验证，可使液体空分产品的单位电耗在原有基础上再降低约7％，使CO 2减排量再增加约7％，有效增大了LNG冷能的利用效益并进一步降低了液体空分产品的成本和设备投资。在设计条件完全相同的情况下，本发明利用液化天然气冷能的空分装置其液体空分产品的单位电耗可从原来的0.36KWh/Nm 3降至0.33Wh/Nm 3左右，是最先进常规流程的约41％，且不消耗冷剂水，是发展循环经济、节能减排的有效举措，具有明显的社会效益和经济效益。
上述实施例只为说明本发明的技术构思及特点，其目的在于让熟悉此项技术的人士能够了解本发明的内容并据以实施，并不能以此限制本发明的保护范围。凡根据本发明精神实质所作的等效变化或修饰，都应涵盖在本发明的保护范围之内。

Claims (12)

  1. 一种利用LNG冷能的空分装置，其特征在于：所述利用LNG冷能的空分装置包括对原料空气进行压缩和净化的空气压缩净化系统、对压缩净化后的原料空气进行精馏而获取空分产品的大冷箱系统、用于实现LNG与为所述大冷箱系统提供冷能的氮之间换热的小冷箱系统、利用出所述小冷箱系统的天然气冷能的制冷剂循环系统、利用出所述制冷剂循环系统的天然气冷能的冷却剂循环系统；
    所述制冷剂循环系统包括通过制冷剂循环通路相连接的制冷剂液化过冷器、制冷剂加压泵、与所述空气压缩净化系统中的原料空气换热的原料空气冷却器以及膨胀发电机组/制冷剂增压透平膨胀机组，出所述小冷箱系统的天然气通过所述制冷剂液化过冷器；所述原料空气冷却器包括中间冷却器和末级冷却器；
    所述冷却剂循环系统包括冷却剂换热器及冷却剂循环泵，出所述制冷剂循环系统的天然气和冷却剂均通过所述冷却剂换热器；
    所述空气压缩净化系统包括依次设置的原料空压机、各级原料空气冷却器和空气纯化器；
    所述大冷箱系统包括依次设置的主换热器和精馏塔系统；
    所述小冷箱系统包括LNG-氮换热器和液氮过冷器；
    由所述大冷箱系统输出的低温低压氮气经低温低压氮压机或所述制冷剂增压透平膨胀机组后送入所述小冷箱系统，由所述大冷箱系统输出的压力氮气也送入所述小冷箱系统。
  2. 一种利用LNG冷能的空分装置，其特征在于：所述利用LNG冷能的空分装置包括对原料空气进行压缩和净化的空气压缩净化系统、对压缩净化后的原料空气进行精馏而获取空分产品的大冷箱系统、用于实现LNG与为所述大冷箱系统提供冷能的氮之间换热的小冷箱系统、利用出所述小冷箱系统的天然气冷能的制冷剂循环系统、利用出所述制冷剂循环系统的天然气冷能的冷却剂循环系统。
  3. 根据权利要求2所述的一种利用LNG冷能的空分装置，其特征在于：所述制冷剂循环系统包括通过制冷剂循环通路相连接的制冷剂液化过冷器、制冷剂加压泵、与所述空气压缩净化系统中的原料空气换热的原料空气冷却器以及膨胀发电机组/制冷剂增压透平膨胀机组，所述出所述小冷箱系统的天然气进入所述制冷剂液化过冷器使制冷剂液化过冷。
  4. 根据权利要求3所述的一种利用LNG冷能的空分装置，其特征在于：所述原料空气冷却器包括中间冷却器和末级冷却器。
  5. 根据权利要求3所述的一种利用LNG冷能的空分装置，其特征在于：所述制冷剂液化过冷器设置在所述小冷箱系统内，或设置在所述小冷箱系统外。
  6. 根据权利要求2所述的一种利用LNG冷能的空分装置，其特征在于：所述冷却剂循环系统包括冷却剂换热器及冷却剂循环泵，出所述制冷剂循环系统的天然气和冷却剂均通过所述冷却剂换热器。
  7. 根据权利要求2所述的一种利用LNG冷能的空分装置，其特征在于：所述空气压缩净化系统包括依次设置的原料空压机、各级原料空气冷却器和空气纯化器。
  8. 根据权利要求2所述的一种利用LNG冷能的空分装置，其特征在于：所述大冷箱系统包括依次设置的主换热器和精馏塔系统。
  9. 根据权利要求2所述的一种利用LNG冷能的空分装置，其特征在于：所述小冷箱系统包括LNG-氮换热器和液氮过冷器。
  10. 根据权利要求9所述的一种利用LNG冷能的空分装置，其特征在于：所述小冷箱系统的氮出口管上设置有报警联锁的碳氢化合物检测仪。
  11. 根据权利要求3所述的一种利用LNG冷能的空分装置，其特征在于：由所述大冷箱系统输出的低温低压氮气经低温低压氮压机或所述制冷剂增压透平膨胀机组后压缩到规定压力后送入所述小冷箱系统。
  12. 一种利用LNG冷能的空分方法，其特征在于：所述空分方法为：梯级利用LNG的冷能，先将LNG送入小冷箱系统中与氮换热，并利用换热后得到的液氮为精馏原料空气而获得空分产品提供冷能；再将出所述小冷箱系统的天然气送入制冷剂循环系统中与制冷剂换热，并利用换热后已液化过冷的制冷剂去冷却压缩后的空气，被空气气化升温后的所述制冷剂去为膨胀发电机组或制冷剂增压透平膨胀机组膨胀做功；最后将出所述制冷剂循环系统的还带有部分冷量的天然气送入冷却剂循环系统中与冷却剂换热，并利用换热后的冷却剂来冷却需冷却的设备。
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Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN113405318A (zh) * 2021-06-29 2021-09-17 杭州制氧机集团股份有限公司 一种使用单个精馏塔生产纯氮的装置及其使用方法
CN114017992A (zh) * 2021-11-09 2022-02-08 四川空分设备(集团)有限责任公司 一种适用于lng冷能负荷变化的空分系统
CN114485056A (zh) * 2022-02-11 2022-05-13 开封黄河空分集团有限公司 一种空分的空气低温冷却液化装置
CN114791205A (zh) * 2022-04-22 2022-07-26 杭州特盈能源技术发展有限公司 一种绿电高效转化低能耗空分储能及co2提纯液化工艺
CN115075988A (zh) * 2022-06-28 2022-09-20 江苏科技大学 大规模低功耗lng动力船舶尾气碳捕集系统及运作方法
CN115342597A (zh) * 2022-07-01 2022-11-15 中国石油化工股份有限公司 一种lng冷能用于空气分离与海水淡化系统及其综合利用方法
CN117722819A (zh) * 2024-02-18 2024-03-19 浙江浙能技术研究院有限公司 一种自平衡式耦合lng冷能的新型液化空气储能系统
CN114485056B (zh) * 2022-02-11 2024-05-10 开封黄河空分集团有限公司 一种空分的空气低温冷却液化装置

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110701870B (zh) * 2019-05-29 2022-07-12 苏州市兴鲁空分设备科技发展有限公司 一种利用lng冷能的空分装置和方法
CN112577261B (zh) * 2020-12-21 2024-04-26 襄阳航力机电技术发展有限公司 天然气降压发电系统及液化天然气的提取方法

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH09138063A (ja) * 1995-11-14 1997-05-27 Osaka Gas Co Ltd 液化天然ガス冷熱利用の空気分離方法および設備
CN101846436A (zh) * 2010-05-27 2010-09-29 中国海洋石油总公司 利用lng冷能的全液体空气分离装置
CN101915495A (zh) * 2010-08-25 2010-12-15 开封空分集团有限公司 利用液化天然气冷能的全液体空气分离装置及方法
CN202675796U (zh) * 2012-04-26 2013-01-16 中国海洋石油总公司 利用lng冷能生产液体空分产品的装置
CN105783424A (zh) * 2016-04-22 2016-07-20 暨南大学 利用液化天然气冷能生产高压富氧气体的空气分离方法
CN105865149A (zh) * 2016-04-22 2016-08-17 暨南大学 一种利用液化天然气冷能生产液态空气的方法
CN110701870A (zh) * 2019-05-29 2020-01-17 苏州市兴鲁空分设备科技发展有限公司 一种利用lng冷能的空分装置和方法

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN201532078U (zh) * 2009-06-04 2010-07-21 中国海洋石油总公司 利用液化天然气冷能的空气分离系统
CN101571340B (zh) * 2009-06-04 2011-02-23 中国海洋石油总公司 利用液化天然气冷能的空气分离方法
CN102032756A (zh) * 2011-01-07 2011-04-27 苏州市兴鲁空分设备科技发展有限公司 空气分离方法
CN104019628B (zh) * 2014-05-14 2016-04-13 中国海洋石油总公司 使空分系统在lng冷能供应中断期间连续运行的方法
CN203824225U (zh) * 2014-05-14 2014-09-10 中国海洋石油总公司 一种可与接收站冷能供应相匹配的空分装置

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH09138063A (ja) * 1995-11-14 1997-05-27 Osaka Gas Co Ltd 液化天然ガス冷熱利用の空気分離方法および設備
CN101846436A (zh) * 2010-05-27 2010-09-29 中国海洋石油总公司 利用lng冷能的全液体空气分离装置
CN101915495A (zh) * 2010-08-25 2010-12-15 开封空分集团有限公司 利用液化天然气冷能的全液体空气分离装置及方法
CN202675796U (zh) * 2012-04-26 2013-01-16 中国海洋石油总公司 利用lng冷能生产液体空分产品的装置
CN105783424A (zh) * 2016-04-22 2016-07-20 暨南大学 利用液化天然气冷能生产高压富氧气体的空气分离方法
CN105865149A (zh) * 2016-04-22 2016-08-17 暨南大学 一种利用液化天然气冷能生产液态空气的方法
CN110701870A (zh) * 2019-05-29 2020-01-17 苏州市兴鲁空分设备科技发展有限公司 一种利用lng冷能的空分装置和方法

Cited By (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN113405318A (zh) * 2021-06-29 2021-09-17 杭州制氧机集团股份有限公司 一种使用单个精馏塔生产纯氮的装置及其使用方法
CN113405318B (zh) * 2021-06-29 2024-04-05 杭氧集团股份有限公司 一种使用单个精馏塔生产纯氮的装置的使用方法
CN114017992A (zh) * 2021-11-09 2022-02-08 四川空分设备(集团)有限责任公司 一种适用于lng冷能负荷变化的空分系统
CN114485056A (zh) * 2022-02-11 2022-05-13 开封黄河空分集团有限公司 一种空分的空气低温冷却液化装置
CN114485056B (zh) * 2022-02-11 2024-05-10 开封黄河空分集团有限公司 一种空分的空气低温冷却液化装置
CN114791205A (zh) * 2022-04-22 2022-07-26 杭州特盈能源技术发展有限公司 一种绿电高效转化低能耗空分储能及co2提纯液化工艺
CN114791205B (zh) * 2022-04-22 2023-07-21 杭州特盈能源技术发展有限公司 一种绿电高效转化低能耗空分储能及co2提纯液化工艺
CN115075988A (zh) * 2022-06-28 2022-09-20 江苏科技大学 大规模低功耗lng动力船舶尾气碳捕集系统及运作方法
CN115075988B (zh) * 2022-06-28 2023-09-15 江苏科技大学 大规模低功耗lng动力船舶尾气碳捕集系统及运作方法
CN115342597A (zh) * 2022-07-01 2022-11-15 中国石油化工股份有限公司 一种lng冷能用于空气分离与海水淡化系统及其综合利用方法
CN117722819A (zh) * 2024-02-18 2024-03-19 浙江浙能技术研究院有限公司 一种自平衡式耦合lng冷能的新型液化空气储能系统
CN117722819B (zh) * 2024-02-18 2024-05-07 浙江浙能技术研究院有限公司 一种自平衡式耦合lng冷能的新型液化空气储能系统

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