WO2019104524A1 - 通过与氮气膨胀机联动制动的膨胀机增压机来产生增压空气的深冷精馏方法与设备 - Google Patents

通过与氮气膨胀机联动制动的膨胀机增压机来产生增压空气的深冷精馏方法与设备 Download PDF

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WO2019104524A1
WO2019104524A1 PCT/CN2017/113525 CN2017113525W WO2019104524A1 WO 2019104524 A1 WO2019104524 A1 WO 2019104524A1 CN 2017113525 W CN2017113525 W CN 2017113525W WO 2019104524 A1 WO2019104524 A1 WO 2019104524A1
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Prior art keywords
expander
air
nitrogen
heat exchanger
pressure
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PCT/CN2017/113525
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English (en)
French (fr)
Chinese (zh)
Inventor
赵伯伟
布里格利亚⋅阿兰
薛凤杰
戴⋅埃里克
Original Assignee
乔治洛德方法研究和开发液化空气有限公司
赵伯伟
布里格利亚⋅阿兰
薛凤杰
戴⋅埃里克
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Application filed by 乔治洛德方法研究和开发液化空气有限公司, 赵伯伟, 布里格利亚⋅阿兰, 薛凤杰, 戴⋅埃里克 filed Critical 乔治洛德方法研究和开发液化空气有限公司
Priority to PCT/CN2017/113525 priority Critical patent/WO2019104524A1/zh
Priority to US16/768,056 priority patent/US20200355429A1/en
Priority to KR1020207016963A priority patent/KR102389110B1/ko
Priority to EP17933288.7A priority patent/EP3719427A4/en
Priority to CN201780097181.6A priority patent/CN111406192B/zh
Publication of WO2019104524A1 publication Critical patent/WO2019104524A1/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
    • F25J3/04406—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
    • 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
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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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    • F25J3/02—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
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    • 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
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    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
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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
    • 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
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04296—Claude expansion, i.e. expanded into the main or high pressure column
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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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    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04309—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
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    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • F25J3/04381—Details relating to the work expansion, e.g. process parameter etc. using work extraction by mechanical coupling of compression and expansion so-called companders
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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
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • F25J3/04387—Details relating to the work expansion, e.g. process parameter etc. using liquid or hydraulic turbine expansion
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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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    • F25J3/02—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
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    • F25J3/04393—Details relating to the work expansion, e.g. process parameter etc. using multiple or multistage gas work expansion
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    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
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    • F25J3/04957—Arrangements of multiple air fractionation units or multiple equipments fulfilling the same process step, e.g. multiple trains in a network and inter-connecting equipments upstream of the fractionation unit (s), i.e. at the "front-end"
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    • F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
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    • F25J2240/46—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval the fluid being oxygen

Definitions

  • the invention relates to a cryogenic rectification air separation process and device.
  • cryogenic rectification to separate air into nitrogen and oxygen is a common and well-skilled technology.
  • At least two air separation columns, the intermediate pressure column and the low pressure column, operating at different pressures are connected in a heat exchange manner through the main condensing evaporator.
  • the pressurized, purified and cooled air feed gas is fed to an intermediate pressure column and/or a low pressure column to obtain gaseous and/or liquid nitrogen and oxygen by rectification. All or part of the nitrogen and oxygen are exchanged with the air gas in the main heat exchanger to obtain nitrogen and oxygen products at normal temperature.
  • the design of air separation units and processes is generally based on customer requirements for nitrogen, oxygen product status, pressure and production.
  • the method is either an internal pressure boosting method in which the low temperature liquid oxygen or liquid nitrogen is raised to the required pressure by a pump and then reheated by the main heat exchanger.
  • the internal pressurization process is generally adopted for the sake of production safety and equipment cost.
  • the high-pressure warm-flow stock is required to evaporate and vaporize the high-pressure liquid oxygen in the main heat exchanger.
  • This warm-flowing stock is generally a high-pressure air gas, and may also be a circulating high-pressure nitrogen gas. If high-pressure air gas is used, the air gas that has passed through the main air compressor to reach the pressure of the intermediate pressure tower is further pressurized by the supercharger to a higher pressure, which is an energy-consuming process.
  • the technical problem to be solved by the present invention is to improve the utilization of the rectification capacity of the air separation column, particularly the low pressure column.
  • a further technical problem to be solved by the present invention is to reduce the energy required to pressurize the air gas. Consumption.
  • Another technical problem to be solved by the present invention is how to flexibly provide nitrogen to customers with different yields and pressures.
  • the invention discloses a method of cryogenically rectifying air to produce nitrogen and oxygen, comprising: providing a column operating at a higher pressure, ie, a medium pressure column, and operating at a lower pressure
  • the two towers that is, the low pressure tower, one tower and two towers are connected by heat exchange through a main condensing evaporator.
  • At least one air pre-cooling system, one air purification system, one main air compressor, at least one air booster, at least one main heat exchanger, and one subcooler are provided.
  • the air gas pressurized by the main air compressor to the first pressure range is further processed by the pre-cooling system and the purification system, and a part of the air is sent to the main heat exchanger to exchange heat with the gas product produced by the rectification.
  • a part of the air After entering a tower, another part of it is pressurized by an air booster and a plurality of stage expander superchargers, and after being exchanged with the gas and liquid products produced by rectification in the main heat exchanger, it is expanded or throttled.
  • After decompressing to the first pressure range it is sent to a tower, or the partially separated liquid is supercooled by a cooler and then sent to the second tower.
  • the air gas is rectified in a column, the oxygen-rich liquid is taken out at the bottom of a column, and the pure liquid nitrogen is taken from the top, and the liquid nitrogen is selectively extracted in the middle, and after being cooled by the cooler, it is sent to the second column as a reflux liquid.
  • the pure liquid oxygen is extracted from the main condensing evaporator, pressurized by the liquid oxygen pump, and sent to the main heat exchanger for heat exchange and evaporation with the air gas after being pressurized by the air booster and the turbocharger of several stages of expanders. Vaporization is output as a product.
  • the nitrogen gas is extracted from the second tower, and after heating through the cooler, it enters the main heat exchanger to further reheat.
  • Pure nitrogen at the pressure of the first nitrogen product is withdrawn from the top of a column and sent to the main heat exchanger for reheating. Wherein, part of the pure nitrogen gas located at the pressure of the first nitrogen product is partially reheated in the main heat exchanger, and then depressurized to a second nitrogen product pressure by a nitrogen expander, and then further reheated by the main heat exchanger to be output as a product.
  • the nitrogen expander is braked by the first expander supercharger, the first expander supercharger further pressurizes the air gas that is partially pressurized by the air booster and reaches the second pressure range to the third pressure Range, the air gas in the third pressure range is directly or optionally further pressurized, and then enters the main heat exchanger to exchange heat with the gas and liquid products produced by the rectification, and is depressurized to a first pressure range by the liquid expander. It is sent to a tower, or part of the liquid is cooled by the cooler and then sent to the second tower.
  • the present invention also discloses an apparatus for cryogenically rectifying air to produce nitrogen and oxygen, comprising: a tower operating at a higher pressure and a second tower operating at a lower pressure, The tower and the second column are connected by heat exchange through a main condensing evaporator. At least one air precooling system, one air purification system, one main air compressor, one air booster, first expander A supercharger, at least one main heat exchanger, a nitrogen expander, at least one liquid expander, a liquid oxygen pump and a subcooler.
  • the air feed gas is fed to the main tower air line through the main air compressor, the air pre-cooling system, the air purification system and the main heat exchanger.
  • the oxygen-enriched liquid at the bottom of one tower is sent to the pipeline of the second tower through the cold of the cooler; the pure liquid nitrogen at the top of one tower is subcooled through the cooler and sent to the pipeline above the second tower; alternatively, one will be
  • the dirty liquid nitrogen in the middle of the tower is sent to the pipeline of the second tower through the cold of the cooler; the sewage nitrogen of the second tower is pumped out to the pipeline which is heated by the subcooler and reheated by the main heat exchanger; the pure liquid oxygen is taken from the main
  • the condensing evaporator is taken out, pressurized by the liquid oxygen pump and passed through the pipeline of the main heat exchanger; pure nitrogen is withdrawn from the top of the lower tower and sent to the pipeline of the main heat exchanger.
  • the method further includes feeding part of the reheated pure nitrogen gas from the main heat exchanger to the nitrogen expander, and returning the expanded pure nitrogen to the reheating pipeline of the main heat exchanger; the nitrogen expander is increased by the first expander.
  • the press brake, the main air compressor, the air booster and the first expander supercharger are connected in series, and pass through the main heat exchanger, and the liquid expander is connected to the lower tower through the pipeline.
  • the nitrogen product is only withdrawn from the top of a column, and the pressure of this nitrogen product is generally a medium pressure of 5 to 6 bara. If the customer requires a higher pressure of nitrogen, the reheated nitrogen can be further pressurized with a supercharger. If the customer desires a lower pressure nitrogen instead of a low pressure nitrogen draw from a pure nitrogen column located at the top of the lower pressure column, the present invention takes the expansion of the medium pressure nitrogen to obtain the desired low pressure nitrogen. Further, the above nitrogen expander may be braked by an expander booster of compressed air. It can be seen that the present invention can flexibly produce nitrogen gas of different pressures, and at the same time, utilizes the work of nitrogen expansion to reduce the energy consumption for producing pressurized air.
  • the amount of pure liquid nitrogen which can be used as the two column reflux liquid will be reduced accordingly. This will make greater use of the rectification capacity of the two towers, and will also reduce the diameter of the two towers required, making transportation of them more convenient.
  • 1 is an embodiment of the present invention in which a first expander supercharger and a second expander supercharger are connected in series.
  • FIG. 2 is a still further embodiment of the present invention in which a parallel manner is employed between the first expander supercharger and the second expander supercharger.
  • Figure 3 is a comparative embodiment of the invention which does not include a nitrogen expander.
  • air gas refers to a mixture comprising primarily oxygen and nitrogen.
  • pure nitrogen covers a gaseous fluid having a nitrogen content of not less than 99 mole percent; the term “soil nitrogen” covers a gaseous fluid having a nitrogen content of not less than 95 mole percent, and the nitrogen content of "soil nitrogen” is less than "pure” Nitrogen”.
  • oxygen-rich liquid space refers to a liquid fluid having a molar percentage of oxygen greater than 30, the term “pure liquid oxygen” covers a liquid fluid having a molar percentage of oxygen greater than 99, and the oxygen content in “pure liquid oxygen” is higher than "rich” Oxygen liquid is empty.”
  • pure liquid nitrogen refers to a liquid fluid having a molar percentage of nitrogen greater than 99
  • stain liquid nitrogen refers to a liquid fluid having a molar percentage of nitrogen greater than 96
  • the content of nitrogen in “soil liquid nitrogen” is less than “pure liquid nitrogen”.
  • the cryogenic rectification of the present disclosure is a rectification process carried out at least in part at a temperature of 150 K or less.
  • “tower” herein is meant a distillation or fractionation column or zone in which the liquid phase and the gas phase are countercurrently contacted to effectively separate the fluid mixture.
  • the operating pressure of the "one column” in the present disclosure is generally 5 to 6.5 bara, which is higher than the general operating pressure of the "two columns” of 1.1 to 1.5 bara.
  • the two towers can be installed vertically on top of one tower or two towers can be installed side by side.
  • the "one tower” is also commonly referred to as the medium pressure tower or the lower tower.
  • the “two towers” are also generally referred to as the low pressure tower or the upper tower.
  • the main condensing evaporator is generally located at the top of the "one tower". It can make the pure nitrogen produced at the top of a tower exchange heat with the pure liquid oxygen generated at the bottom of the two towers to obtain pure liquid nitrogen at the top of a tower. The liquid oxygen partially evaporates.
  • the type of the main condensing evaporator includes a shell-and-tube type, a falling film type, a bath type, and the like, and a dip-type condensing evaporator can be employed in the present invention.
  • the air pre-cooling system of the present invention is used to pre-cool the high temperature air (70-120 ° C) discharged from the main air compressor to a temperature suitable for entering the air purification system (typically 10-25 ° C).
  • the high-temperature air is generally in contact with the ordinary circulating cooling water and the low-temperature water (generally 5-20 ° C) in the air cooling tower to achieve heat transfer.
  • the low temperature water can be obtained by heat exchange of ordinary circulating cooling water with a gas product or by-product produced by an air separation plant, such as a nitrogen gas, or by a freezer.
  • the air purification system refers to a purification device that removes dust, water vapor, CO 2 , hydrocarbons, and the like in the air.
  • a pressure swing adsorption mode is generally employed in which the adsorbent is optionally a molecular sieve plus alumina or only a molecular sieve.
  • the compressed, pre-cooled, purified air gas and the gas and/or liquid products produced by the rectification are subjected to non-contact heat exchange and are cooled to a rectification temperature close to or equal to one column, generally Below 150K.
  • Common main heat exchangers include split or integrated.
  • the main heat exchanger is divided into a high pressure (>20 bara pressure) and a low pressure ( ⁇ 20 bara pressure) heat exchanger according to a suitable pressure range.
  • a high pressure plate heat exchanger and a low pressure plate heat exchanger or an integral combined heat exchanger can be used at the same time.
  • the first pressure range is consistent with the operating pressure range of a column or medium pressure column, typically 5-6 bara, and the air gas at atmospheric pressure can be compressed by the main air compressor to reach this pressure range.
  • the second pressure range is a pressure range that is reached after the air gas in the first pressure range is pressurized by the air booster, and is generally 40 to 60 bara.
  • the third pressure range is achieved by further pressurizing the air feed gas in the second pressure range via the first expander supercharger and/or the second expander supercharger, typically 60 to 75 bara.
  • the air gas in the second and third pressure ranges needs to be able to exchange heat with the pressurized liquid oxygen in the main heat exchanger and evaporate and vaporize, so that its specific pressure is determined by the pressure of the liquid oxygen that needs to be vaporized. .
  • the first nitrogen product pressure refers to the pressure of pure nitrogen extracted from the top of a column or a medium pressure column, and is generally 4 to 5 bara. According to the customer's needs, the pure nitrogen gas having the pressure of the first nitrogen product can be expanded and decompressed to obtain the pressure of the second nitrogen product, generally ⁇ 1.1 bara; or the pure nitrogen gas having the pressure of the first nitrogen product can be passed through the nitrogen booster.
  • the pressure of the third nitrogen product is obtained after pressurization, generally greater than 7 bara.
  • the pressure of the second and third nitrogen products can be flexibly determined according to the needs of the customer.
  • the Rahman principle states that when pure oxygen is produced using the upper or lower pressure column, the rectification capacity of the low pressure column is not fully utilized.
  • one or more of the following measures are employed to improve this situation, thereby increasing the efficiency of the entire air separation system, reducing energy consumption, and even reducing the volume of the tower.
  • One of the measures is to directly introduce part of the air gas into the upper tower, that is, the low pressure tower, thereby utilizing the excess rectification capacity of the tower; the second measure is to take out the pure nitrogen gas generated at the top of the medium pressure tower as a nitrogen product, correspondingly, The amount of pure liquid nitrogen obtained after condensation of the main condenser is reduced, that is, the amount of reflux liquid delivered to the lower pressure column is reduced.
  • the reduction of the reflux liquid further utilizes the rectification capacity of the low pressure column.
  • the reduction of the reflux liquid reduces the processing capacity of the low pressure column, and the diameter of the low pressure column can be correspondingly reduced, which is more convenient for transportation.
  • the pressure of pure nitrogen taken from the top of the intermediate pressure column is generally 4 to 5 bara compared to the pure nitrogen gas having a pressure of about 1 to 2 bara taken from the top of the lower pressure column as a nitrogen product.
  • the pressure of the nitrogen product required by the customer is greater than 4 to 5 bara, such as 10 bara
  • the energy consumption for boosting the pure nitrogen extracted from the medium pressure column to 10 bara is greatly reduced compared to the energy consumption for boosting the pure nitrogen extracted from the low pressure column to 10 bara.
  • the customer needs a nitrogen product pressure of less than 4 to 5 bara, such as 1 bara
  • the pure nitrogen extracted from the medium pressure column can be expanded to 1 bara, and the expansion work can be used to generate electricity or
  • the shaft-coupled expander booster reduces the energy consumption of the entire air separation system.
  • a part of 101 is introduced into the low-pressure main heat exchanger 1 and after rectification.
  • the medium-pressure pure nitrogen gas 123 is partially indirectly heat-exchanged, cooled to about -170 ° C, and sent to the lower portion of a column 11 for rectification.
  • the other portion 102 is further pressurized by the air booster 22 to about 52 bara and is divided into two, one of which 103 is pressurized by the first expander supercharger 24 to become a 58 bara stream 105, and is completely It is sent to the second expander supercharger 26, and further pressurized to a 77 bara stream 106; the other 104 of the 102 is sent to the high pressure main heat exchanger 2, partially cooled, extracted from the center, and expanded by air. After the machine 25 is decompressed to 6 bara, it is also sent to the lower portion of a column 11 for rectification. Since the stream 105 entering the second expander compressor 26 is from the first expander booster 24, the two are connected in series.
  • the first expander supercharger 24 and the second expander supercharger 26 are associated with the nitrogen expander 23 and the air expander 25, respectively, and absorb the work done by the expander.
  • the stream 106 pressurized to 77 bara enters the high pressure main heat exchanger 2 and indirectly exchanges with the pure liquid oxygen 122 after pressurization to 88 bara and part of the dirty liquid nitrogen 121, and the high pressure pure liquid oxygen is condensed to the liquid. 122 evaporates and is exported as a high pressure oxygen product.
  • the condensed air gas After the condensed air gas is decompressed to 6 bara by the liquid expander 28, it is separated into gas-liquid two phases, and the gaseous stream 107 is directly sent to the lower portion of a column 11, and a portion of the liquid stream 108 is cooled by the cooler 3. It is then sent to the middle of the second tower 13.
  • the air feed gas introduced into a column 11 is rectified in a column to form an oxygen-rich liquid space 110 at the bottom of the column and pure nitrogen gas at the top of the column.
  • part of the pure nitrogen is condensed into pure liquid nitrogen.
  • a part of the pure liquid nitrogen described above is optionally supplied as a liquid nitrogen product to the storage tank, and the other portion 112 is cooled and then introduced into the upper portion of the second column 13 as a reflux liquid.
  • the cold input to the second column also includes an oxygen-rich liquid space 110, and optionally, a dirty liquid nitrogen 111 and a portion of the liquid air gas 108 extracted from the middle of a column 11.
  • the above-mentioned stream is depressurized to a pressure of about 1.3 to 1.4 bara and then sent to the second column 13.
  • the sewage nitrogen gas 121 having a pressure of about 1.3 bara can be extracted in the upper part of the second tower.
  • Pure liquid oxygen 122 having a pressure of about 1.4 bara was obtained at the bottom.
  • the pure liquid oxygen can be boosted to about 88 bara by the liquid oxygen pump 31 and then vaporized by the high pressure air gas 106, 104 in the high pressure main heat exchanger 2 to obtain a high pressure oxygen product. .
  • a partial high-pressure liquid oxygen can be depressurized after the liquid oxygen pump to obtain a medium-pressure liquid oxygen with a pressure of about 30 bara, similarly, in the high-pressure main heat exchanger 2 Evaporated and vaporized by high pressure air gas 106, 104 from And get medium pressure oxygen products.
  • the only nitrogen product is medium pressure pure nitrogen 123 with a pressure of about 5.5 bara drawn from the top of a column 11.
  • the following operations can be performed.
  • a portion 124 of the partially reheated medium pressure pure nitrogen gas 123 is withdrawn and depressurized to a desired pressure by a nitrogen expander 23, referred to as a second nitrogen product pressure, followed by It is returned to the main heat exchanger and completely reheated to obtain a second nitrogen product.
  • the nitrogen expander 23 is braked by the first expander supercharger 24 to convert the expansion work into the energy required to compress the air feed.
  • the low-pressure main heat exchanger 1 After the remaining part of the medium-pressure pure nitrogen gas 123 is completely reheated by the low-pressure main heat exchanger 1, it can be used as the first nitrogen product, the pressure output of the first nitrogen product, or the pressure boosted by the nitrogen booster to the customer's required Three nitrogen product pressures are output as a third nitrogen product.
  • the main difference between the embodiment shown in Fig. 2 and Fig. 1 is the connection relationship between the first expander compressor 24 and the second expander compressor 26, and in Fig. 2, the two are in parallel. Specifically, after the pre-cooling and purification system is purified by the pre-cooling system pre-cooling and purification system through the main air compressor 21, a part of 101 is introduced into the low-pressure main heat exchanger 1 and after rectification.
  • the medium-pressure pure nitrogen gas 123 is partially indirectly heat-exchanged, cooled to about -170 ° C, and sent to the lower portion of a column 11 for rectification.
  • the other portion 102 is further pressurized to about 52 bara by the air booster 22 and is divided into three strands, one of which is pressurized by the first expander supercharger 24 to become a 76 bara stream 116;
  • a 117 is sent to the high pressure main heat exchanger 2, partially cooled and then withdrawn from the central portion.
  • After being fed into the second expander supercharger 26 it is also pressurized to a 76 bara stream 119 which, after mixing with 116, enters the high pressure main heat exchanger 2, and with pure liquid oxygen 122 and a portion after pressurization to 88 bara.
  • the dirty liquid nitrogen 121 indirectly exchanges heat, and partially vaporizes the liquid to vaporize the high-pressure pure liquid oxygen 122 and output it as a high-pressure oxygen product. Since the streams entering the first and second expander compressors are each from the boost end of the air booster 22, the two are connected in parallel. After the condensed air gas 120 is depressurized to 6 bara by the liquid expander 28, it can be divided into two by a gas-liquid separator, and one gaseous stream 107 is directly sent to the lower part of one column 11, and the other liquid stream is 108 is cooled by the cooler 3 and sent to the middle of the second tower 13.
  • the first expander supercharger 24 and the second expander supercharger 26 are associated with the nitrogen expander 23 and the air expander 25, respectively, and absorb the work done by the expander.
  • FIG. 2 the process flow shown in FIG. 2 is taken as an embodiment according to the present invention
  • FIG. 3 the process flow shown in FIG. 3 is taken as a comparative example.
  • Fig. 3 is provided with a pure nitrogen column 14 at the upper portion of the two columns, and a low pressure pure nitrogen gas 140 having a pressure of about 1.3 bara is directly extracted from the top of the pure nitrogen column.
  • the low pressure pure nitrogen gas 140 is reheated by the cooler 3 and the main heat exchanger 1 and then output as a second nitrogen product.
  • Fig. 3 the process flow shown in FIG. 2 is taken as an embodiment according to the present invention
  • FIG. 3 is taken as a comparative example.
  • Fig. 3 is provided with a pure nitrogen column 14 at the upper portion of the two columns, and a low pressure pure nitrogen gas 140 having a pressure of about 1.3 bara is directly extracted from the top of the pure nitrogen column.
  • the low pressure pure nitrogen gas 140 is reheated by the cooler 3 and the main heat exchanger 1 and then output
  • medium pressure pure nitrogen 123 having a pressure of about 5.5 bara is still withdrawn from the top of a column, but all of the stream is reheated by the main heat exchanger 1 as a first nitrogen product, or alternatively, The part is output as a third nitrogen product after further pressurization.
  • the comparative example of Fig. 3 does not have a nitrogen expander 23 and a first expander supercharger 24 associated therewith. Specifically, after the air gas pressurized to 6 bara by the main air compressor 21 is purified by the pre-cooling system 301 pre-cooling and purification system 302, a portion of 101 enters the low-pressure main heat exchanger 1 and after rectification.
  • the obtained medium-pressure pure nitrogen gas 123, a part of the sewage nitrogen gas 121 and the low-pressure pure nitrogen gas 140 are indirectly exchanged, cooled to about -170 ° C, and sent to the lower portion of a column 11 for rectification.
  • the other portion 102 is further pressurized to about 51 bara by the air booster 22 and is divided into two, one of which is sent to the high pressure main heat exchanger 2, partially cooled and then withdrawn from the center, through the air expander 25 is reduced to 6 bara of stream 132 and then sent to the lower part of a column 11 for rectification; the other 133 is pressurized by the second expander supercharger 26 to 76 bara and then enters the high pressure main heat exchanger 2, and
  • the indirect heat exchange with the pure liquid oxygen 122 after pressurization to 88 bara and a portion of the dirty liquid nitrogen 121 causes the high pressure pure liquid oxygen 122 to be vaporized and vaporized as a high pressure oxygen product while partially condensing to the liquid.
  • the condensed air gas After the condensed air gas is depressurized to 6 bara by the liquid expander 28, it can be divided into two by a gas-liquid separator, and one gaseous stream 107 is directly sent to the lower portion of one column 11, and the other liquid stream 108 is discharged. After being cooled by the cooler 3, it is sent to the middle of the second tower 13.
  • the rest of the comparative examples are the same as the embodiment shown in Fig. 2.
  • the simulation calculations listed in the table below were performed using ASPEN software for a space division system with an oxygen production of 100,000 Nm 3 /h.
  • the main heat exchanger is aluminum plate-fin type, and the main air compressor (MAC) and air booster (BAC) are high-pressure steam-driven steam turbines.
  • the operating cost is calculated based on the price of high pressure steam of 100 RMB/ton and is evaluated on a 5-year basis.
  • the O 2 recovery obtained according to the present invention is slightly lower than that of the comparative example, but the loss here is more comprehensive than the energy saving obtained by the present invention. It must be a lot smaller.
  • the “medium-pressure pure nitrogen extraction amount” in the above table refers to the flow rate of medium-pressure pure nitrogen extracted from the top of a column
  • the “low-pressure pure nitrogen extraction amount” refers to the flow rate of low-pressure pure nitrogen extracted from the top of the pure nitrogen column
  • the flow rate of the medium-pressure pure nitrogen gas to the low-pressure pure nitrogen gas refers to the flow rate of the portion of the medium-pressure pure nitrogen gas which is taken out from the middle portion of the main heat exchanger and fed into the nitrogen gas expander 23.
  • the work performed by the nitrogen expander since the work performed by the nitrogen expander is utilized, the work required to generate the air gas of the final substantially the same pressure and flow rate by the air booster (BAC) is reduced, and the corresponding high-pressure steam is also consumed. decreased. A total of five years, can save about 10 million operating costs.

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PCT/CN2017/113525 2017-11-29 2017-11-29 通过与氮气膨胀机联动制动的膨胀机增压机来产生增压空气的深冷精馏方法与设备 WO2019104524A1 (zh)

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US16/768,056 US20200355429A1 (en) 2017-11-29 2017-11-29 Cryogenic distillation method and apparatus for producing pressurized air by means of expander booster in linkage with nitrogen expander for braking
KR1020207016963A KR102389110B1 (ko) 2017-11-29 2017-11-29 제동을 위한 질소 팽창기와 연결된 팽창기 부스터에 의해 가압된 공기를 생산하기 위한 극저온 증류 방법 및 장치
EP17933288.7A EP3719427A4 (en) 2017-11-29 2017-11-29 CRYOGENIC DISTILLATION PROCESS AND DEVICE FOR GENERATING COMPRESSED AIR BY USING AN EXPANDER-BOOSTER IN COMBINATION WITH A NITROGEN EXPANDER FOR BRAKING
CN201780097181.6A CN111406192B (zh) 2017-11-29 2017-11-29 通过与氮气膨胀机联动制动的膨胀机增压机来产生增压空气的深冷精馏方法与设备

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