CN118532889A - Cryogenic air separation plant and method for cryogenically separating air - Google Patents

Cryogenic air separation plant and method for cryogenically separating air Download PDF

Info

Publication number
CN118532889A
CN118532889A CN202410718297.9A CN202410718297A CN118532889A CN 118532889 A CN118532889 A CN 118532889A CN 202410718297 A CN202410718297 A CN 202410718297A CN 118532889 A CN118532889 A CN 118532889A
Authority
CN
China
Prior art keywords
pressure
air
product
liquid
heat exchanger
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
Application number
CN202410718297.9A
Other languages
Chinese (zh)
Inventor
邢博
曹建伟
陈燕清
郑好转
孙连明
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Original Assignee
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Priority to CN202410718297.9A priority Critical patent/CN118532889A/en
Publication of CN118532889A publication Critical patent/CN118532889A/en
Pending legal-status Critical Current

Links

Classifications

    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02Processes 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
    • F25J3/04Processes 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
    • F25J3/04006Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04109Arrangements of compressors and /or their drivers
    • F25J3/04115Arrangements of compressors and /or their drivers characterised by the type of prime driver, e.g. hot gas expander
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02Processes 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
    • F25J3/04Processes 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
    • F25J3/04006Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078Providing 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
    • F25J3/0409Providing 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
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02Processes 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
    • F25J3/04Processes 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
    • F25J3/04151Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04163Hot end purification of the feed air
    • F25J3/04169Hot end purification of the feed air by adsorption of the impurities
    • F25J3/04175Hot end purification of the feed air by adsorption of the impurities at a pressure of substantially more than the highest pressure column
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02Processes 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
    • F25J3/04Processes 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
    • F25J3/04151Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04242Cold end purification of the feed air
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02Processes 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
    • F25J3/04Processes 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
    • F25J3/04248Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284Generation 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
    • F25J3/0429Generation 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
    • F25J3/04296Claude expansion, i.e. expanded into the main or high pressure column
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02Processes 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
    • F25J3/04Processes 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
    • F25J3/04406Processes 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
    • F25J3/04412Processes 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
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00Processes characterised by the type or other details of the feed stream
    • F25J2210/40Air or oxygen enriched air, i.e. generally less than 30mol% of O2

Landscapes

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

Abstract

The invention provides a cryogenic air separation plant and a method of cryogenically separating air having a main air compressor, a single expansion turbine, and a turbocharger, main heat exchanger and rectifying column system driven thereby. The method for separating air at low temperature is suitable for the situation that the pressure of the first product after internal compression is not higher than 6bara, and the range of the liquid production ratio is 20% -30%. The feed air is compressed in a main air compressor to a first pressure air stream at least 6bara above the operating pressure of the higher pressure column, a first portion of the first pressure air stream is compressed in a turbocharger to form a second pressure air stream, the second pressure air stream is partially cooled in the main heat exchanger and then directed to an expansion turbine, and after expansion depressurization, is directed to a rectification column system; the second part of the first pressure air stream is fed into the rectification column system after being completely cooled in the main heat exchanger and throttled and depressurized. The air separation plant of the invention does not comprise an air booster driven by externally supplied energy.

Description

低温空气分离设备和低温分离空气的方法Low temperature air separation equipment and method for low temperature air separation

技术领域Technical Field

本发明属于空气分离领域,涉及一种低温分离空气的方法和低温空气分离装置,尤其涉及一种采用内压缩流程获得带压气体产物的低温分离空气的方法和设备。The present invention belongs to the field of air separation, and relates to a method and a device for low-temperature air separation, and in particular to a method and a device for low-temperature air separation which adopt an internal compression process to obtain a pressurized gas product.

背景技术Background Art

通过低温精馏空气生产氧气、氮气、氩气等空气产品是一种已知的技术。低温精馏的空气分离设备一般包括主空气压缩机、空气预冷和纯化系统、主热交换器和精馏塔系统,并利用从外部引入深冷液体(例如液氮)或采用空气膨胀产生低温分离所需要的冷量。精馏塔系统可包括单塔,或通过热交换的形式联接的双塔及三塔等。作为示例,双塔形式的精馏塔系统由操作压力分别相对较低和较高的低压塔和高压塔组成,并能同时生产气态及液态的氮气和氧气等产品。It is a known technology to produce air products such as oxygen, nitrogen, argon, etc. by low-temperature distillation of air. The air separation equipment of low-temperature distillation generally includes a main air compressor, an air precooling and purification system, a main heat exchanger and a distillation tower system, and uses the introduction of cryogenic liquid (such as liquid nitrogen) from the outside or the use of air expansion to generate the cold required for low-temperature separation. The distillation tower system may include a single tower, or a double tower and a triple tower connected by heat exchange. As an example, a double-tower distillation tower system consists of a low-pressure tower and a high-pressure tower with relatively low and high operating pressures, respectively, and can simultaneously produce gaseous and liquid nitrogen and oxygen products.

当客户需要压力高于高压塔或低压塔的操作压力的气体产品时,现有技术中采用外压缩或内压缩流程。外压缩流程是指将从精馏塔中取出的液态或气态产物,在不改变其压力的情况下,在主热交换器中汽化(针对液态产物)及复热,并将相应的复热后的气态产物用气体压缩机压缩到客户需要的压力的气体产品的流程。When the customer needs a gas product with a pressure higher than the operating pressure of the high-pressure tower or the low-pressure tower, the prior art uses an external compression or internal compression process. The external compression process refers to the process of vaporizing (for liquid products) and reheating the liquid or gaseous product taken out of the distillation tower in the main heat exchanger without changing its pressure, and compressing the corresponding reheated gaseous product to the pressure required by the customer using a gas compressor.

内压缩流程是指将从精馏塔中取出的液态产物,用液体泵将其压力升高到客户需要的压力,然后在主热交换器中蒸发、伪蒸发及复热,得到压力合适的气体产品的流程。The internal compression process refers to the process of increasing the pressure of the liquid product taken out of the distillation tower to the pressure required by the customer by using a liquid pump, and then evaporating, pseudo-evaporating and reheating it in the main heat exchanger to obtain a gas product with appropriate pressure.

当客户需要的气体产品为压力氧气产品时,出于安全性和氧气利用率的考虑,将液氧流股用液氧泵提升至客户所需的压力,再在主热交换器中使用正流的高压空气将其汽化并复热的内压缩流程是优选的。现有技术中往往在主空气压缩机后再使用空气增压机来获得正流的高压空气,例如US5,515,687、CN108253732A中,都公开了将至少一部分经主空气压缩机压缩、预冷纯化后的空气,在常温状态下,在由外部提供能量的再压缩机(即空气增压机)中压缩到压力高于待汽化液氧压力的正流的高压空气的方法。When the gas product required by the customer is a pressure oxygen product, for the sake of safety and oxygen utilization, the internal compression process of raising the liquid oxygen stream to the pressure required by the customer with a liquid oxygen pump, and then using the positive flow of high-pressure air in the main heat exchanger to vaporize and reheat it is preferred. In the prior art, an air booster is often used after the main air compressor to obtain a positive flow of high-pressure air. For example, US5,515,687 and CN108253732A both disclose a method of compressing at least a portion of the air compressed, pre-cooled and purified by the main air compressor in a re-compressor (i.e., an air booster) provided with energy from the outside to a positive flow of high-pressure air with a pressure higher than the pressure of the liquid oxygen to be vaporized at room temperature.

鉴于低温空气分离工艺一般投资和能耗都很可观,为了提高生产效率,降低能耗,节约投资和运营费用,本领域技术人员致力于针对特定的产品类型,优化工艺流程。In view of the fact that the investment and energy consumption of the cryogenic air separation process are generally considerable, in order to improve production efficiency, reduce energy consumption, and save investment and operating costs, technical personnel in this field are committed to optimizing the process flow for specific product types.

发明内容Summary of the invention

本发明意在提供一种低温分离空气的方法以及低温空气分离设备,从而更有效和成本更有利地生产一定压力及组成的液体和气体产品。The present invention is directed to a method for cryogenically separating air and a cryogenic air separation plant, thereby more efficiently and cost-effectively producing liquid and gas products of a given pressure and composition.

为了实现上述发明目的,在一方面,本发明公开了一种低温分离空气的方法,采用空气分离设备,空气分离设备具有主空气压缩机、空气预冷和纯化系统、唯一的膨胀涡轮机、唯一的涡轮增压器、主热交换器和具有一高压塔和一低压塔的精馏塔系统。涡轮增压器由膨胀涡轮机驱动。首先,在主空气压缩机中将所有的进料空气压缩至第一空气压力,形成第一压力空气流,第一空气压力比所述高压塔的操作压力高至少6bara;然后,将第一压力空气流的第一部分在所述涡轮增压器中压缩至第二空气压力,形成第二压力空气流,第二压力空气流在所述主热交换器中部分冷却后,导入所述膨胀涡轮机,膨胀降压后输入所述精馏塔系统;同时,将第一压力空气流的第二部分在所述主热交换器中完全冷却,节流降压后输入所述精馏塔系统;。在所述空气分离设备中获得液体产物,所述空气分离设备的产液比的范围为20%~30%。在所述精馏塔系统中获得液态的第一产物流,该第一产物流以液态状态被提升到更高的第一产物压力,在所述主热交换器中与第一压力空气流的第二部分换热,被蒸发或者伪蒸发和复热后,作为第一压力气体产物从所述空气分离设备中去除,其中,所述空气分离设备不包含由外部供应的能量驱动的空气增压机。In order to achieve the above-mentioned invention object, on one hand, the present invention discloses a method for low-temperature separation of air, which uses an air separation device, and the air separation device has a main air compressor, an air precooling and purification system, a single expansion turbine, a single turbocharger, a main heat exchanger and a distillation tower system having a high-pressure tower and a low-pressure tower. The turbocharger is driven by the expansion turbine. First, all the feed air is compressed to a first air pressure in the main air compressor to form a first pressure air flow, and the first air pressure is at least 6 bara higher than the operating pressure of the high-pressure tower; then, the first part of the first pressure air flow is compressed to a second air pressure in the turbocharger to form a second pressure air flow, and the second pressure air flow is partially cooled in the main heat exchanger, introduced into the expansion turbine, expanded and depressurized, and then input into the distillation tower system; at the same time, the second part of the first pressure air flow is completely cooled in the main heat exchanger, throttled and depressurized, and then input into the distillation tower system; a liquid product is obtained in the air separation device, and the liquid production ratio of the air separation device ranges from 20% to 30%. A liquid first product stream is obtained in the distillation tower system, which is raised to a higher first product pressure in a liquid state, heat-exchanged with a second part of the first pressure air stream in the main heat exchanger, evaporated or pseudo-evaporated and reheated, and then removed from the air separation device as a first pressure gas product, wherein the air separation device does not include an air booster driven by externally supplied energy.

在上述方法中,第一空气压力的范围为12bara~17bara,第二空气压力的范围为17bara~25bara。In the above method, the first air pressure ranges from 12 bara to 17 bara, and the second air pressure ranges from 17 bara to 25 bara.

进一步地,第一产物流包含液氧,第一产物压力不高于6bara,第一压力气体产物为氧气;优选地,第一产物压力不高于4.5bara。Further, the first product stream comprises liquid oxygen, the first product pressure is not higher than 6 bara, and the first pressure gas product is oxygen; preferably, the first product pressure is not higher than 4.5 bara.

上述方法生产的液体产物包含液氧、液氮或液氩中的一种或多种。The liquid product produced by the above method comprises one or more of liquid oxygen, liquid nitrogen or liquid argon.

在另一方面,本发明公开了一种低温空气分离设备,包含:主热交换器;具有一高压塔和一低压塔的精馏塔系统;主空气压缩机,特征在于使所有的进料空气压缩至第一空气压力,并形成第一压力空气流,所述第一空气压力比所述高压塔的操作压力高至少6bara;唯一的涡轮增压器,其由所述的膨胀涡轮机驱动,用于将所述第一压力空气流的第一部分压缩至第二空气压力,并形成第二压力空气流;唯一的膨胀涡轮机,其用于接受在主热交换器中部分冷却后的第二压力空气流;用于将第一压力空气流的第二部分导入主热交换器,完全冷却后,节流降压导入所述精馏塔系统的器件;用于将膨胀降压后的第二压力空气流导入所述精馏塔系统的器件。用于将所述精馏塔系统中获得的液态的第一产物流,提升到更高的第一产物压力的装置;将位于第一产物压力的液态的第一产物流在所述主热交换器中与第一压力空气流的第二部分换热,以及将被蒸发或者伪蒸发和加热后形成的第一压力气体产物从所述空气分离设备中去除的器件;将所述精馏塔系统中获得的液体产物从所述空气分离设备中去除的器件,所述空气分离设备的产液比的范围为20%~30%;特别地,所述空气分离设备不包含由外部供应的能量驱动的空气增压机。On the other hand, the present invention discloses a low-temperature air separation device, comprising: a main heat exchanger; a distillation tower system having a high-pressure tower and a low-pressure tower; a main air compressor, characterized in that it compresses all feed air to a first air pressure and forms a first pressure air flow, and the first air pressure is at least 6 bara higher than the operating pressure of the high-pressure tower; a unique turbocharger, which is driven by the expansion turbine and is used to compress a first part of the first pressure air flow to a second air pressure and form a second pressure air flow; a unique expansion turbine, which is used to receive the second pressure air flow after partial cooling in the main heat exchanger; a device for introducing the second part of the first pressure air flow into the main heat exchanger, and after complete cooling, throttling and reducing the pressure to introduce it into the distillation tower system; a device for introducing the second pressure air flow after expansion and reduction of pressure into the distillation tower system. A device for raising the liquid first product stream obtained in the distillation tower system to a higher first product pressure; a device for exchanging heat between the liquid first product stream at the first product pressure and the second part of the first pressure air stream in the main heat exchanger, and removing the first pressure gas product formed after evaporation or pseudo-evaporation and heating from the air separation device; a device for removing the liquid product obtained in the distillation tower system from the air separation device, the liquid ratio of the air separation device ranging from 20% to 30%; in particular, the air separation device does not include an air booster driven by externally supplied energy.

本发明设计了一种简洁高效的空分流程,通过低温空气分离得到气体及液体产物,其中气体产物(特别是氧气)的压力不高于6bara,液体产物的产液比的范围在20%~30%。与传统的空分流程相比,除主空气压缩机之外,本发明未采用空气增压机,只采用了一个用膨胀涡轮机带动的涡轮增压器,从而节省了投资和能耗。The present invention designs a simple and efficient air separation process, which obtains gas and liquid products through low-temperature air separation, wherein the pressure of the gas product (especially oxygen) is not higher than 6 bara, and the liquid ratio of the liquid product is in the range of 20% to 30%. Compared with the traditional air separation process, in addition to the main air compressor, the present invention does not use an air compressor, but only uses a turbocharger driven by an expansion turbine, thereby saving investment and energy consumption.

附图说明BRIEF DESCRIPTION OF THE DRAWINGS

关于本发明的优点与精神可以通过以下的发明详述及附图得到进一步的了解。The advantages and spirit of the present invention can be further understood through the following detailed description of the invention and the accompanying drawings.

图1是本发明所提供的实施例1的流程示意图。FIG1 is a schematic diagram of a flow chart of Example 1 provided by the present invention.

图中:20-主空气压缩机;21-空气预冷纯化系统;22-涡轮增压器;23-膨胀涡轮机;24-后冷却器;25-主热交换器;26-节流阀;27-液体泵;28-冷凝蒸发器;29-高压塔;30-低压塔;50-精馏塔系统;1-进料空气;2-第一压力空气流;3-第一压力空气流的第一部分;4-第二压力空气流;5-第一压力空气流的第二部分;6-第一产物流;7-氮气;8-污氮气;9-液氧;10-液氮;11-第一压力气体产物;100-空气分离设备。In the figure: 20-main air compressor; 21-air precooling and purification system; 22-turbocharger; 23-expansion turbine; 24-aftercooler; 25-main heat exchanger; 26-throttle valve; 27-liquid pump; 28-condenser evaporator; 29-high-pressure tower; 30-low-pressure tower; 50-distillation tower system; 1-feed air; 2-first pressure air flow; 3-first part of the first pressure air flow; 4-second pressure air flow; 5-second part of the first pressure air flow; 6-first product flow; 7-nitrogen; 8-dirty nitrogen; 9-liquid oxygen; 10-liquid nitrogen; 11-first pressure gas product; 100-air separation equipment.

具体实施方式DETAILED DESCRIPTION

下面结合附图详细说明本发明的具体实施例。然而,应当将本发明理解成并不局限于以下描述的这种实施方式,并且本发明的技术理念可以与其他公知技术或功能与那些公知技术相同的其他技术组合实施。The specific embodiments of the present invention are described in detail below in conjunction with the accompanying drawings. However, the present invention should be understood to be not limited to the embodiments described below, and the technical concept of the present invention can be implemented in combination with other known technologies or other technologies with the same functions as those known technologies.

术语“第一”、“第二”仅用于描述目的,并非是指对时间顺序、数量、或者重要性的限定,不能理解为指示或暗示相对重要性或者隐含指明所指示的技术特征的数量,而仅仅是为了将本技术方案中的一个技术特征与另一个技术特征相区分。由此,限定有“第一”、“第二”的特征可以明示或隐含地包括一个或多个该特征。在本发明的描述中,“多个”的含义是两个或两个以上,除非另有明确具体的规定。同样地,本文中出现的类似于“一”的限定语并非是指对数量的限定,而是描述在前文中未曾出现的技术特征。同样地,除非是有特定的数量量词修饰的名词,否则在本文中应当视作既包含单数形式又包含复数形式,在该技术方案中既可以包括单数个该技术特征,也可以包括复数个该技术特征。“唯一”及“仅、只”等词语应被理解为特定的数量量词,表示它们所限定的名词有且只有一个。The terms "first" and "second" are used only for descriptive purposes and do not refer to the limitation of time sequence, quantity, or importance. They cannot be understood as indicating or implying relative importance or implicitly indicating the number of indicated technical features, but are only for distinguishing one technical feature from another technical feature in the technical solution. Therefore, the features defined as "first" and "second" can explicitly or implicitly include one or more of the features. In the description of the present invention, the meaning of "multiple" is two or more, unless otherwise clearly and specifically specified. Similarly, the qualifiers similar to "one" appearing in this article do not refer to the limitation of quantity, but describe technical features that have not appeared in the previous text. Similarly, unless it is a noun modified by a specific quantitative quantifier, it should be regarded as including both singular and plural forms in this article, and the technical solution can include both singular and plural technical features. Words such as "only" and "only" should be understood as specific quantitative quantifiers, indicating that there is only one noun defined by them.

本文中在数词前出现的类似于“大约”、“近似地”的修饰语通常包含本数,并且其具体的含义应当结合上下文意理解。数词作为一个数值范围的端点出现时,该数值范围包含两个端点的数值;相似地,数值作为一个开放式范围的一个端点时,例如与“至少”、“至多”、“不大于”、“不小于”、“不高于”、“不低于”相连时,该开放式数值范围亦包含端点的数值。In this article, modifiers such as "about" and "approximately" that appear before a numeral usually include the number itself, and their specific meanings should be understood in conjunction with the context. When a numeral appears as an endpoint of a numerical range, the numerical range includes the values of both endpoints; similarly, when a numerical value is an endpoint of an open-ended range, such as when it is connected with "at least", "at most", "not more than", "not less than", "not higher than", or "not lower than", the open-ended numerical range also includes the values of the endpoints.

应当理解,在本发明中,“至少一个(次)”是指一个(次)或者多个(次)。“和/或”用于描述关联对象的关联关系,表示可以存在三种关系,例如,“A和/或B”可以表示:只存在A,只存在B以及同时存在A和B三种情况,其中A,B可以是单数或者复数。It should be understood that in the present invention, "at least one (time)" means one (time) or more (times). "And/or" is used to describe the association relationship of associated objects, indicating that three relationships may exist. For example, "A and/or B" can mean: only A exists, only B exists, and both A and B exist, where A and B can be singular or plural.

如本文所用,术语“和/或”包括一个或多个相关列出项的任意和全部组合。除非另有说明,否则本文所用的所有术语(包括技术和科学术语)的含义与本发明所属领域的普通技术任意通常所理解的含义相同。还应理解的是,术语,诸如常用字典中定义的那些,应被理解为具有与其在本说明书及相关领域的上下文中的含义一致的含义,并且不应以理想化或过度正式的意义来理解,除非本文汇总明确有此规定。为了简洁和/或清晰起见,熟知的功能或构造可能不会详细描述。As used herein, the term "and/or" includes any and all combinations of one or more of the associated listed items. Unless otherwise specified, all terms (including technical and scientific terms) used herein have the same meaning as any commonly understood meaning in the ordinary art of the field to which the invention belongs. It should also be understood that terms, such as those defined in common dictionaries, should be understood to have a meaning consistent with their meaning in the context of this specification and the related art, and should not be understood in an idealized or overly formal sense unless otherwise specified herein. For the sake of brevity and/or clarity, well-known functions or configurations may not be described in detail.

在这里,在压力数据中通常不包含自然压力损失。如果相应部位之间的压力差不大于由管道、热交换器、冷却器、吸附器、普通调节阀(非节流阀)等中的压力损失导致的自然线路损失,则压力在这里被评为“相等”。本发明中的“压力”、“压力范围”可容纳一定的误差,其使用的单位为绝对压力。对于一套特定的低温空气分离设备或低温空气分离流程,各压力范围不相重合。Here, natural pressure losses are usually not included in the pressure data. If the pressure difference between the corresponding parts is not greater than the natural line loss caused by the pressure loss in the pipeline, heat exchanger, cooler, adsorber, ordinary regulating valve (non-throttle valve), etc., the pressure is rated as "equal" here. The "pressure" and "pressure range" in the present invention can accommodate a certain error, and the unit used is absolute pressure. For a specific set of cryogenic air separation equipment or cryogenic air separation process, the pressure ranges do not overlap.

本发明中的空气分离设备100是指接受进料空气的馈入,并能产生气体产物和液体产物的一套装置的组合。其中进料空气为常温常压的未经纯化的空气,气体产物一般为通过换热器复热到常温,且压力和纯度满足要求的气态产品,液体产物一般为未经复热的,压力和纯度满足要求的液态产品。液体产物往往直接输入管网或贮存容器。直接作为产品从空气分离设备中取出的液体产物的产量越高,该套空气分离设备需要的冷量越多。实践中用产液比表征空气分离设备中所有液体产物相对氧产物的摩尔比值,液体产物可以包含液氧(LOX)、液氮(LIN)或在有氩产品的情况下,液氩(LAR),氧产品包含液氧(LOX)和气氧(GOX),其计算方式如下:The air separation device 100 in the present invention refers to a combination of a set of devices that receive feed air and can produce gas products and liquid products. The feed air is unpurified air at room temperature and pressure, the gas product is generally a gaseous product that is reheated to room temperature through a heat exchanger and whose pressure and purity meet the requirements, and the liquid product is generally a liquid product that is not reheated and whose pressure and purity meet the requirements. The liquid product is often directly input into a pipeline network or a storage container. The higher the output of the liquid product directly taken out of the air separation device as a product, the more cooling capacity the air separation device requires. In practice, the liquid production ratio is used to characterize the molar ratio of all liquid products relative to oxygen products in the air separation device. The liquid product can include liquid oxygen (LOX), liquid nitrogen (LIN) or, in the case of argon products, liquid argon (LAR). The oxygen product includes liquid oxygen (LOX) and gaseous oxygen (GOX), and the calculation method is as follows:

本发明中的精馏塔系统是指接受低温进料空气的馈入,通过气液传质的方式将空气分离成气态或液态的氧、氮等成分的装置。精馏塔系统50以高度简化的形式示出,包括安装于冷箱中的塔体和安装于塔内的各设备,例如塔板、填料、冷凝蒸发器等;连接各塔,以及将精馏产物输出的管道和阀门等。精馏塔系统50包括至少一个在1.0bara~3.0bara的压力水平下操作的低压塔30和在4.0bara~7.0bara的压力水平下操作的高压塔29,其中低压塔和高压塔经由主冷凝蒸发器28进行热联接。The distillation tower system in the present invention refers to a device that receives low-temperature feed air and separates the air into gaseous or liquid oxygen, nitrogen and other components by gas-liquid mass transfer. The distillation tower system 50 is shown in a highly simplified form, including a tower body installed in a cold box and various equipment installed in the tower, such as tower plates, packings, condenser evaporators, etc.; pipes and valves connecting the towers and outputting the distillation products, etc. The distillation tower system 50 includes at least one low-pressure tower 30 operating at a pressure level of 1.0 bara to 3.0 bara and a high-pressure tower 29 operating at a pressure level of 4.0 bara to 7.0 bara, wherein the low-pressure tower and the high-pressure tower are thermally connected via a main condenser evaporator 28.

“压缩机”在本发明中指被用于将至少一种气流从进入压缩机时的起始压力压缩到将所述流从压缩机中取出的最终压力的装置。安装在一个壳体中的一个压缩机可以包含单个或多个压缩级。主空气压缩机压缩进料到空气分离设备中空气量的全部或主要部分,即全部进料空气流。将在主空气压缩机中被压缩的进料空气的部分或全部压缩到更高的压力的压缩机称为再压缩机或空气增压机。在本发明中,空气增压机特指全部由外部供应的能量驱动的压缩机,即不是通过在空气分离设备中先前压缩的流体的膨胀而驱动的增压机。本发明的空气分离设备中不包含上述定义的空气增压机。"Compressor" in the present invention refers to a device used to compress at least one gas flow from the initial pressure when entering the compressor to the final pressure at which the flow is withdrawn from the compressor. A compressor installed in a housing may contain a single or multiple compression stages. The main air compressor compresses all or a major part of the amount of air fed into the air separation device, that is, the entire feed air flow. A compressor that compresses part or all of the feed air compressed in the main air compressor to a higher pressure is called a recompressor or air booster. In the present invention, an air booster specifically refers to a compressor that is driven entirely by externally supplied energy, that is, a booster that is not driven by the expansion of a fluid previously compressed in the air separation device. The air booster defined above is not included in the air separation device of the present invention.

空气预冷系统设置在主空气压缩机的下游,采用空冷塔、水冷塔、冷冻机或相组合的方式将进料空气冷却到10℃~25℃的范围,并送入空气纯化系统。空气纯化系统的目的是移除进料空气中的水、二氧化碳、碳氢化合物等可能在深冷状态下冻结的物质,一般常采用填充有分子筛和氧化铝等吸附剂的平行设置的吸附器。The air precooling system is set at the downstream of the main air compressor, and uses air cooling tower, water cooling tower, refrigerator or a combination of them to cool the feed air to the range of 10℃~25℃, and then send it to the air purification system. The purpose of the air purification system is to remove water, carbon dioxide, hydrocarbons and other substances in the feed air that may freeze under cryogenic conditions. Generally, parallel adsorbers filled with adsorbents such as molecular sieves and alumina are often used.

“主热交换器”用于在与来自精馏塔系统的返回流间接热交换中冷却进料空气,如与污氮气或低温空气分离产物换热。主热交换器可以由单个热交换区段或并联和/或串联连接的多个热交换区段形成,其具有被设计为彼此分开并具有热交换表面的流体通道的“通道”。完全冷却指的是被冷却的流股在热端进入主热交换器,然后从冷端引出主热交换器,即该流股流经的通道贯穿整个主热交换器;而部分冷却是指被冷却的流股从热端与冷端中间的位置引出主热交换器,即该流股流经的通道未贯穿整个主热交换器。The "main heat exchanger" is used to cool the feed air in indirect heat exchange with the return stream from the distillation column system, such as heat exchange with dirty nitrogen or cryogenic air separation products. The main heat exchanger can be formed by a single heat exchange section or a plurality of heat exchange sections connected in parallel and/or in series, which have "channels" designed as fluid channels separated from each other and having heat exchange surfaces. Full cooling means that the cooled stream enters the main heat exchanger at the hot end and then is led out of the main heat exchanger from the cold end, that is, the channel through which the stream flows runs through the entire main heat exchanger; while partial cooling means that the cooled stream is led out of the main heat exchanger from a position between the hot end and the cold end, that is, the channel through which the stream flows does not run through the entire main heat exchanger.

“膨胀涡轮机”或“膨胀机”,用于膨胀具有压力的气态或至少是部分液态的流股,并在此过程中做功。在本发明中,膨胀涡轮机23经由共用轴与涡轮增压器22相耦合,从而驱动涡轮增压器22。在理想的状态下,膨胀涡轮机所做的功全部地传递给机械连接的相应的涡轮增压器,而不使用例如通过电动机外部供应的能量。机械连接在这里的语境中被理解为通过机械部件,例如齿轮、皮带、变速器等类似装置在这些旋转部件之间实现固定的或机械可调的转速关系。在本发明中,仅使用一个膨胀涡轮机和一个完全由其驱动的涡轮增压器。An "expansion turbine" or "expander" is used to expand a gaseous or at least partially liquid stream under pressure and to perform work in the process. In the present invention, the expansion turbine 23 is coupled to the turbocharger 22 via a common shaft, thereby driving the turbocharger 22. In an ideal state, the work performed by the expansion turbine is entirely transferred to the corresponding mechanically connected turbocharger without using energy supplied externally, for example, by an electric motor. Mechanical connection in this context is understood to mean a fixed or mechanically adjustable speed relationship between these rotating parts by mechanical components, such as gears, belts, transmissions and the like. In the present invention, only one expansion turbine and a turbocharger driven entirely by it are used.

在图1代表的实施例1中,进料空气1首先在主空气压缩机20中被压缩到第一空气压力,并生成第一压力空气流2。第一空气压力比高压塔的操作压力高至少6bara,即第一空气压力的范围为12bara~17bara。在空气预冷和纯化系统21中去除杂质后,第一压力空气流2分成两部分,第一部分3被涡轮增压器22进一步压缩到第二空气压力,并形成第二压力空气流4。在涡轮增压器22后可以设置用冷却水冷却的后冷却器24,从而将压缩热移出空气分离设备100。第二压力空气流4在主热交换器25中部分冷却后,进入膨胀涡轮机23,膨胀泄压至高压塔29的压力后,被馈入高压塔。第一压力空气流2的第二部分5在主热交换器25中完全冷却后,经节流器26泄压至精馏塔系统50的操作压力后,被馈入相应的高压塔和/或低压塔。In the embodiment 1 represented in FIG. 1 , the feed air 1 is first compressed to a first air pressure in the main air compressor 20 and generates a first pressure air stream 2. The first air pressure is at least 6 bara higher than the operating pressure of the high pressure column, that is, the first air pressure ranges from 12 bara to 17 bara. After impurities are removed in the air precooling and purification system 21, the first pressure air stream 2 is divided into two parts, and the first part 3 is further compressed to a second air pressure by the turbocharger 22 to form a second pressure air stream 4. An aftercooler 24 cooled by cooling water can be provided after the turbocharger 22 to remove the heat of compression from the air separation device 100. After the second pressure air stream 4 is partially cooled in the main heat exchanger 25, it enters the expansion turbine 23, expands and releases to the pressure of the high pressure column 29, and is fed into the high pressure column. After the second part 5 of the first pressure air stream 2 is completely cooled in the main heat exchanger 25, it is released to the operating pressure of the distillation column system 50 through the throttle 26, and is fed into the corresponding high pressure column and/or low pressure column.

实施例1的精馏塔生成包含液氧9和液氮10的液体产物,二者被引出精馏塔系统50后,不再作为返流参与主热交换器25中的换热。还生成污氮气8和纯氮气7,二者以气态的形式在主热交换器中复热后,可作为产品取出或实现预冷、再生纯化器的功能。流股6是液态的第一产物流,在本实例中为液氧,也可以根据需要为液氮或液氩等。液体泵27被设置成将第一产物流的压力提升到更高的压力,增压后的流股6在主热交换器25中蒸发或伪蒸发及复热后,作为第一压力气体产物11从空气分离设备中移出。The distillation tower of Example 1 generates liquid products including liquid oxygen 9 and liquid nitrogen 10. After being led out of the distillation tower system 50, the two no longer participate in the heat exchange in the main heat exchanger 25 as reflux. Dirty nitrogen gas 8 and pure nitrogen gas 7 are also generated. After being reheated in the main heat exchanger in gaseous form, they can be taken out as products or realize the functions of precooling and regenerating the purifier. Stream 6 is a liquid first product stream, which is liquid oxygen in this example, and can also be liquid nitrogen or liquid argon as required. The liquid pump 27 is configured to increase the pressure of the first product stream to a higher pressure. The pressurized stream 6 is evaporated or pseudo-evaporated and reheated in the main heat exchanger 25, and then removed from the air separation device as a first pressure gas product 11.

为了在主热交换器中汽化增压后的第一产物流,需向该主热交换器提供一压力和流量相匹配的常温空气流股。在本发明中,这一流股是第一压力空气流2的第二部分5。当第一产物流为液氮或液氩时,第一空气压力大致与升压后的第一产物流的压力,即第一产物压力相等;当第一产物流为液氧时,第一空气压力与升压后得到的第一产物压力呈倍数关系,例如2倍。本发明特别适合第一产物压力不高于6bara,优选地不高于4.5bara,此时第一空气压力的范围在12bara~17bara。In order to vaporize the pressurized first product stream in the main heat exchanger, a normal temperature air stream with matching pressure and flow rate needs to be provided to the main heat exchanger. In the present invention, this stream is the second part 5 of the first pressure air stream 2. When the first product stream is liquid nitrogen or liquid argon, the first air pressure is roughly equal to the pressure of the first product stream after pressurization, that is, the first product pressure; when the first product stream is liquid oxygen, the first air pressure is a multiple of the first product pressure obtained after pressurization, for example, 2 times. The present invention is particularly suitable for the first product pressure not higher than 6 bara, preferably not higher than 4.5 bara, and the first air pressure ranges from 12 bara to 17 bara.

在实施例1中,以第一压力气体产物为氧气为例,液体产物为液氧流9与液氮流10,氧产品为液氧流9与第一压力气体产物11,产液比的计算方法为,采用各流股的摩尔数:In Example 1, taking the first pressure gas product as oxygen as an example, the liquid products are liquid oxygen stream 9 and liquid nitrogen stream 10, and the oxygen product is liquid oxygen stream 9 and the first pressure gas product 11. The calculation method of the production-liquid ratio is to use the molar number of each stream:

当空气分离设备的产液比的范围为20%~30%,特别是在20%~25%之间时,采用本发明的方法和设备是特别有益的。通过选择合适的第一空气压力和第二空气压力,使得涡轮增压器完全由膨胀涡轮机做的功带动,减少了能耗和购买额外的空气增压机的投资。When the liquid production ratio of the air separation device is in the range of 20% to 30%, especially between 20% and 25%, the method and device of the present invention are particularly beneficial. By selecting the appropriate first air pressure and the second air pressure, the turbocharger is completely driven by the work done by the expansion turbine, thereby reducing energy consumption and the investment in purchasing an additional air compressor.

本说明书中所述的只是本发明的较佳具体实施例,以上实施例仅用以说明本发明的技术方案而非对本发明的限制。凡本领域技术人员依本发明的构思通过逻辑分析、推理或者有限的实验可以得到的技术方案,皆应在本发明的范围之内。The preferred specific embodiments of the present invention are described in this specification. The above embodiments are only used to illustrate the technical solutions of the present invention and are not intended to limit the present invention. Any technical solutions that can be obtained by those skilled in the art through logical analysis, reasoning or limited experiments according to the concept of the present invention should be within the scope of the present invention.

Claims (6)

1.一种低温分离空气的方法,采用空气分离设备,所述空气分离设备具有主空气压缩机、空气预冷和纯化系统、唯一的膨胀涡轮机、唯一的涡轮增压器、主热交换器和精馏塔系统,所述精馏塔系统具有一高压塔和一低压塔,所述涡轮增压器由所述膨胀涡轮机驱动,其特征在于,1. A method for cryogenically separating air, using an air separation device, wherein the air separation device has a main air compressor, an air precooling and purification system, a single expansion turbine, a single turbocharger, a main heat exchanger and a distillation column system, wherein the distillation column system has a high-pressure column and a low-pressure column, and the turbocharger is driven by the expansion turbine, characterized in that: -所有的进料空气在主空气压缩机中被压缩至第一空气压力,形成第一压力空气流,所述第一空气压力比所述高压塔的操作压力高至少6bara,- all feed air is compressed in the main air compressor to a first air pressure to form a first pressure air stream, wherein the first air pressure is at least 6 bara higher than the operating pressure of the high pressure column, -所述第一压力空气流的第一部分在涡轮增压器中被再压缩至第二空气压力,形成第二压力空气流,所述第二压力空气流在主热交换器中部分冷却后,被导入膨胀涡轮机,膨胀降压后输入所述精馏塔系统,- a first part of the first pressure air flow is recompressed to a second air pressure in a turbocharger to form a second pressure air flow, and the second pressure air flow is partially cooled in a main heat exchanger and then introduced into an expansion turbine, expanded and depressurized, and then introduced into the distillation column system, -所述第一压力空气流的第二部分在主热交换器中完全冷却后,进一步降压后输入所述精馏塔系统,- the second part of the first pressure air flow is completely cooled in the main heat exchanger and then further reduced in pressure before being fed into the distillation column system, -在所述空气分离设备中获得液体产物,所述空气分离设备的产液比的范围为20%-30%,- obtaining a liquid product in the air separation device, wherein the liquid product ratio of the air separation device is in the range of 20% to 30%, -在所述精馏塔系统中获得液态的第一产物流,该第一产物流以液态状态被提升到更高的第一产物压力,在所述主热交换器中与第一压力空气流的第二部分换热,被蒸发或者伪蒸发和复热后,作为第一压力气体产物从所述空气分离设备中去除,- a first liquid product stream is obtained in the rectification column system, the first product stream is raised in liquid state to a higher first product pressure, heat-exchanged with the second part of the first pressure air stream in the main heat exchanger, evaporated or pseudo-evaporated and reheated, and then removed from the air separation device as a first pressure gas product, 其中,in, 所述空气分离设备不包含由外部供应的能量驱动的空气增压机。The air separation plant does not contain an air compressor driven by externally supplied energy. 2.如权利要求1所述低温分离空气的方法,其特征在于,所述第一空气压力的范围为12bara~17bara,所述第二空气压力的范围为17bara~25bara。2. The method for low-temperature separation of air according to claim 1, characterized in that the first air pressure ranges from 12 bara to 17 bara, and the second air pressure ranges from 17 bara to 25 bara. 3.如权利要求2所述低温分离空气的方法,其特征在于,所述第一产物流包含液氧,所述第一产物压力不高于6bara。3. The method for cryogenically separating air according to claim 2, characterized in that the first product stream comprises liquid oxygen and the first product pressure is not higher than 6 bara. 4.如权利要求3所述低温分离空气的方法,其特征在于,所述第一产物压力不高于4.5bara。4. The method for cryogenically separating air according to claim 3, characterized in that the first product pressure is not higher than 4.5 bara. 5.如权利要求1所述低温分离空气的方法,其特征在于,所述液体产物包含液氧、液氮或液氩中的一种或多种。5. The method for cryogenically separating air according to claim 1, wherein the liquid product comprises one or more of liquid oxygen, liquid nitrogen or liquid argon. 6.一种低温空气分离设备,其特征在于,包含:6. A cryogenic air separation device, characterized in that it comprises: -主热交换器,- Main heat exchanger, -精馏塔系统,所述精馏塔系统具有一高压塔和一低压塔,a distillation column system having a high-pressure column and a low-pressure column, -主空气压缩机,用于使所有的进料空气压缩至第一空气压力,并形成第一压力空气流,所述第一空气压力比所述高压塔的操作压力高至少6bara,a main air compressor for compressing all feed air to a first air pressure and forming a first pressure air stream, wherein the first air pressure is at least 6 bara higher than the operating pressure of the high pressure column, -唯一的涡轮增压器,其由膨胀涡轮机驱动,其用于将所述第一压力空气流的第一部分压缩至第二空气压力,并形成第二压力空气流,a single turbocharger, driven by the expansion turbine, for compressing a first portion of the first pressure air flow to a second air pressure and forming a second pressure air flow, -唯一的膨胀涡轮机,其用于接受在主热交换器中部分冷却后的第二压力空气流,- a single expansion turbine adapted to receive the second pressure air stream after it has been partially cooled in the main heat exchanger, -用于将第一压力空气流的第二部分导入主热交换器,完全冷却后,节流降压导入所述精馏塔系统的器件,- a device for introducing the second part of the first pressure air flow into the main heat exchanger, after complete cooling, throttling and reducing the pressure to introduce it into the distillation column system, -用于将膨胀降压后的第二压力空气流导入所述精馏塔系统的器件,- a device for introducing the second pressure air stream after expansion and decompression into the distillation column system, -用于将所述精馏塔系统中获得的液态的第一产物流,提升到更高的第一产物压力的装置,- means for raising the liquid first product stream obtained in the rectification column system to a higher first product pressure, -将位于第一产物压力的液态的第一产物流在所述主热交换器中与第一压力空气流的第二部分换热,以及将被蒸发或者伪蒸发和复热后形成的第一压力气体产物从所述空气分离设备中去除的器件,- means for exchanging heat in the main heat exchanger the first product stream in a liquid state at the first product pressure with the second part of the first pressure air stream, and for removing the first pressure gaseous product formed after evaporation or pseudo-evaporation and reheating from the air separation plant, -将所述精馏塔系统中获得的液体产物从所述空气分离设备中去除的器件,所述空气分离设备的产液比的值的区间为20%-30%,- a device for removing the liquid product obtained in the distillation column system from the air separation device, the liquid production ratio of the air separation device having a value interval of 20%-30%, 其中,in, 所述空气分离设备不包含外部供应的能量驱动的空气增压机。The air separation plant does not contain an air compressor driven by externally supplied energy.
CN202410718297.9A 2024-06-04 2024-06-04 Cryogenic air separation plant and method for cryogenically separating air Pending CN118532889A (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN202410718297.9A CN118532889A (en) 2024-06-04 2024-06-04 Cryogenic air separation plant and method for cryogenically separating air

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN202410718297.9A CN118532889A (en) 2024-06-04 2024-06-04 Cryogenic air separation plant and method for cryogenically separating air

Publications (1)

Publication Number Publication Date
CN118532889A true CN118532889A (en) 2024-08-23

Family

ID=92382676

Family Applications (1)

Application Number Title Priority Date Filing Date
CN202410718297.9A Pending CN118532889A (en) 2024-06-04 2024-06-04 Cryogenic air separation plant and method for cryogenically separating air

Country Status (1)

Country Link
CN (1) CN118532889A (en)

Similar Documents

Publication Publication Date Title
CN111141110B (en) Low-energy-consumption medium-pressure nitrogen preparation process
US20160025408A1 (en) Air separation method and apparatus
WO2021043182A1 (en) Air separation apparatus and method using lng cold energy
CN111406192B (en) Cryogenic rectification method and apparatus for producing pressurized air by expander booster braked in conjunction with nitrogen expander
CN103827612A (en) Air separation method and apparatus
JPH08175806A (en) Method and plant for manufacturing gaseous oxygen under pressure
EP2176610B1 (en) Process for the separation of air by cryogenic distillation
CN101268326A (en) Process and apparatus for the separation of air by cryogenic distillation
WO2019127343A1 (en) Method and device for producing air product based on cryogenic rectification
US6257020B1 (en) Process for the cryogenic separation of gases from air
CN100581996C (en) Device and method for separating pressized nitrogen gas from air
US20150114037A1 (en) Air separation method and apparatus
TW201637998A (en) Method and apparatus for obtaining a compressed nitrogen product
CN111433545B (en) Utilization of nitrogen-rich streams produced in air separation units comprising a split core main heat exchanger
CN107606875A (en) The method and apparatus that compressed nitrogen and liquid nitrogen are produced by low temperature air separating
CN115485519A (en) Integrated nitrogen liquefier for cryogenic air separation units producing nitrogen and argon
TWI663373B (en) Method and apparatus for the cryogenic separation of air
CN104792113A (en) Helium liquefier and control method thereof
US20160153711A1 (en) Method and system for air separation using a supplemental refrigeration cycle
CN1038514A (en) Produce the air separating technological of hyperbaric oxygen and elevated pressure nitrogen
CN118532889A (en) Cryogenic air separation plant and method for cryogenically separating air
TW202108222A (en) Method and system for low-temperature air separation
CN118654448A (en) Low temperature air separation equipment and method for low temperature air separation
CN115060041B (en) System and method for producing nitrogen by liquid-air supercooling, backflow and expansion double towers
US20160245585A1 (en) System and method for integrated air separation and liquefaction

Legal Events

Date Code Title Description
PB01 Publication
PB01 Publication
SE01 Entry into force of request for substantive examination
SE01 Entry into force of request for substantive examination