CN113465292B - Method for increasing yield of krypton/xenon in air rectification device - Google Patents

Method for increasing yield of krypton/xenon in air rectification device Download PDF

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CN113465292B
CN113465292B CN202110756618.0A CN202110756618A CN113465292B CN 113465292 B CN113465292 B CN 113465292B CN 202110756618 A CN202110756618 A CN 202110756618A CN 113465292 B CN113465292 B CN 113465292B
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air
krypton
xenon
evaporator
rectification device
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CN113465292A (en
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阿兰·布里格利亚
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04109—Arrangements of compressors and /or their drivers
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/0423—Subcooling of liquid process streams
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
    • F25J3/04054—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—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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    • 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
    • F25J3/04248—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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • 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
    • F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low 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
    • F25J3/044—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 single pressure main column system only
    • 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
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04745—Krypton and/or Xenon
    • 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
    • F25J3/04763—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
    • F25J3/04951—Arrangements of multiple air fractionation units or multiple equipments fulfilling the same process step, e.g. multiple trains in a network
    • F25J3/04963—Arrangements of multiple air fractionation units or multiple equipments fulfilling the same process step, e.g. multiple trains in a network and inter-connecting equipment within or downstream of the fractionation unit(s)
    • 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/72—Refluxing the column with at least a part of the totally condensed overhead gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/04—Mixing or blending of fluids with the feed stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/50—Oxygen
    • 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
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/34—Krypton
    • 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
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/36—Xenon
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/50—Processes or apparatus involving steps for recycling of process streams the recycled stream being oxygen

Abstract

The invention discloses a method for increasing yield of krypton/xenon in an air rectification device, which comprises the following steps: providing a set of first air rectification means that separates a first feed air stream to produce a krypton/xenon product; providing at least one second air rectification device having a condenser evaporator, the condenser evaporator of the second air rectification device continuously or intermittently producing a condenser evaporator drain; collecting and vaporizing the condensate evaporator drainage liquid, mixing the vaporized condensate evaporator drainage liquid with a first supply air flow, and separating in a first air rectification device to obtain a krypton/xenon product; wherein the flow ratio of the vaporised condenser evaporator drain to the first supply air stream is no more than 1%, preferably no more than 0.5%.

Description

Method for increasing yield of krypton/xenon in air rectification device
Technical Field
The invention belongs to the field of air separation, and relates to the field of air separation for preparing krypton and/or xenon.
Background
Krypton and xenon have important applications in the fields of industry, medicine and the like, and the main source of the krypton and xenon is the atmosphere. One common way of extracting krypton and xenon is from the by-products of air separation plants. Since krypton and xenon are only present in trace amounts in the atmosphere, and only 1.135ppm and 0.086ppm by volume, respectively, this makes it necessary for the air separation unit for extracting krypton and xenon to handle large amounts of feed air to obtain small amounts of product.
The air separation for obtaining krypton and xenon is a mature technology. For example, CN1502552a discloses a method and apparatus for producing a mixture of krypton and xenon from air. Wherein a liquid oxygen stream containing a major portion of krypton and xenon is vaporized after rectification, the gaseous oxygen obtained is reacted with at least one hydrocarbon to produce a synthesis gas containing no more than 0.1ppm (mole) oxygen, and finally components other than krypton and xenon are removed from the synthesis gas. This method reduces the risk of producing explosive hydrocarbon/oxygen ratios during the liquid oxygen enrichment process.
CN102016470A discloses a method for producing krypton and xenon by low-temperature distillation separation of air in double columns (medium-pressure column and low-pressure column), which is mainly characterized in that rich liquid rich in oxygen, krypton and xenon is discharged from the bottom of the medium-pressure column, partial evaporation is carried out in a condensation evaporator to concentrate the rich liquid, and finally the effect of extracting about 90% of xenon and 75% of krypton in gaseous air is achieved, and compared with the extraction rate of about 70% of xenon and 60% of krypton in the traditional method, the extraction rate is improved to a certain extent.
The feed air of the prior art is pressurized, precooled and purified common air consistent with atmospheric components, and the efficiency or safety of extracting krypton and xenon is improved by changing an air separation process and/or a device, wherein the change is complex, and the improvement effect is limited.
In view of this, a task to be solved by the related technical personnel in the industry is urgent, how to design a new process flow to eliminate the above defects and shortcomings in the prior art and to improve the yield of krypton and xenon.
Disclosure of Invention
The invention aims to solve the technical problem of how to greatly improve the yield of krypton and xenon under the condition of hardly changing the process flow and equipment in the conventional cryogenic air rectification system for producing krypton and xenon.
The invention aims to solve another technical problem of how to avoid wasting the fluids containing primarily enriched krypton and xenon for the air separation device with smaller scale which is not suitable for krypton and xenon production.
In order to achieve the above object, the present invention discloses a method for increasing the yield of krypton/xenon, comprising providing a first feed air stream and a first air rectification device, wherein the first feed air stream is separated in the first air rectification device to obtain krypton/xenon product; providing at least one second air rectification device with a condensing evaporator, wherein the condensing evaporator of the second air rectification device generates condensing evaporator drainage liquid; collecting and vaporizing the condensed evaporator liquid discharge, mixing the vaporized condensed evaporator liquid discharge with a first supply air flow, and separating in a first air rectification device to obtain a krypton/xenon product; wherein the flow ratio of the vaporised condenser evaporator drain to the first supply air stream is not more than 1%, preferably not more than 0.5%.
Further, the first air rectification plant comprises a main air compressor, and the vaporized condensate evaporator drain is mixed with the first feed air stream at the inlet end of the main air compressor.
The first air rectification device comprises a main air separation unit, a poor krypton extraction unit, an impurity removal unit, a crude krypton preparation unit, a pure krypton and/or crude xenon preparation unit and an optional crude xenon refining unit.
The second air distillation device can be an air distillation device which does not produce liquid oxygen, such as a nitrogen generator which only produces nitrogen and/or an air distillation device which produces oxygen gas products by adopting an external compression mode. Such air rectification units produce condensate evaporator drains continuously or intermittently during normal operation. The second air rectification device can also only produce the liquid discharge of the condensation evaporator during the maintenance and the emptying. In general, the discharged liquid of the condensing evaporator accounts for 0.1-0.2% of the total amount of the air processed by the second air rectifying device.
Furthermore, the second air rectification device can comprise a plurality of condensation evaporator drainage liquids generated by one or more second air rectification devices, and the condensation evaporator drainage liquids are conveyed to the first air rectification device through pipelines or tank cars.
Compared with the prior art, the technical scheme provided by the invention has the following advantages:
the air rectification plant with smaller scale can process a small amount of feed air, and correspondingly has low content of krypton and xenon, so that the further extraction of krypton and xenon from liquid oxygen, gas oxygen or other byproducts thereof is not feasible from the aspects of economy and technology. For some processes which do not produce liquid oxygen, in order to avoid the explosion hazard caused by the accumulation of hydrocarbons in the condensing evaporator, especially the main condensing evaporator, it is necessary to continuously or intermittently discharge liquid from the condensing evaporator, wherein the main component of the discharged liquid of the condensing evaporator is liquid oxygen and contains a small amount of hydrocarbons and trace amounts of krypton and xenon. In the prior art, the liquid discharge is generally reheated and then directly discharged into the ambient air. The invention collects the liquid discharge from one or more related devices, recovers the primarily enriched krypton and xenon, reduces waste and saves energy.
Because the content of krypton and xenon in the discharged liquid of the condensation evaporator is far higher than that in the atmosphere, even if a small amount of discharged liquid is vaporized and then mixed with feed air to be input into a large-scale air rectification device for producing krypton and xenon, the yield of krypton and xenon in the device can be greatly increased, and the extraction efficiency is improved.
The air flow of the feeding air of the air rectification device for producing krypton and xenon is generally far larger than the flow of the discharged liquid of the condensation evaporator after vaporization, when the ratio of the discharged liquid of the condensation evaporator after vaporization to the feeding air of the condensation evaporator after vaporization is less than 1 percent, preferably less than 0.5 percent, the discharged liquid of the condensation evaporator after vaporization can be mixed with the feeding air of the condensation evaporator at the inlet end of the main air compressor, the equipment selection of the condensation evaporator is not needed, and the process design is very convenient to change.
Drawings
The advantages and spirit of the present invention can be further understood by the following detailed description of the invention and the accompanying drawings.
FIG. 1 is a schematic diagram depicting the flow of the present invention;
FIG. 2 is a schematic diagram of a nitrogen generator of the present invention producing condensing evaporator discharge;
FIG. 3 is a schematic of an external compression process for producing oxygen gas with condensate evaporator drainage according to the present invention.
Detailed Description
Specific embodiments of the present invention will be described in detail below with reference to the accompanying drawings. However, it is to be understood that the present invention is not limited to such an embodiment described below, and the technical idea of the present invention may be implemented in combination with other known techniques or other techniques functionally equivalent to those known techniques.
In the following description of specific embodiments, the present invention will be described with reference to numerous directional terms in order to clearly illustrate the process and apparatus of the present invention, but the terms "upper", "lower", "front", "rear", "outer", "inner", "outward", "inward", and the like should be construed as words of convenience and not as words of limitation.
Furthermore, the terms "first" and "second" are used for descriptive purposes only and are not intended to limit the temporal order, quantity, or importance, but are not intended to indicate or imply relative importance or implicitly indicate the number of technical features indicated, but merely to distinguish one technical feature from another technical feature in the present disclosure. Thus, a feature defined as "first" or "second" may explicitly or implicitly include one or more of that feature. In the description of the present invention, "a plurality" means two or more unless specifically stated otherwise. Similarly, the appearances of the phrases "a" or "an" in various places herein are not intended to be limiting, but rather to describe various features not expressly shown or described in connection with the above description. Similarly, unless a specific number of a claim recitation is intended to cover both the singular and the plural, and embodiments may include a single feature or a plurality of features. Similarly, modifiers similar to "about", "approximately" or "approximately" that occur before a numerical term herein typically include the same number, and their specific meaning should be read in conjunction with the context.
Unless clearly indicated to the contrary, each aspect or embodiment defined herein may be combined with any other aspect or embodiments. In particular, any feature indicated as being preferred or advantageous may be combined with any other feature indicated as being preferred or advantageous.
The adoption of an air rectification device to extract krypton and xenon from the air is a mature technology. Several methods for extracting krypton and xenon are described in detail in "low temperature technology principles and apparatus (bottom)" published by mechanical industry publishers (pages 109-116, first edition 1987), the contents of which are incorporated herein by reference. Krypton and xenon are high boiling components in air, and are generally dissolved in liquid or gaseous oxygen in air separation. From the liquid oxygen or gas oxygen stream, the krypton and xenon products are obtained through the working procedures of extracting poor krypton, removing hydrocarbons in the poor krypton, removing carbon dioxide and moisture in the poor krypton, preparing crude krypton, preparing pure krypton and crude xenon, refining the crude xenon and the like.
Fig. 1 shows an embodiment of the invention comprising a first air rectification device for extracting krypton and xenon from air. After the first supply air is compressed to a suitable pressure (typically 5 to 8 bar) by the main air compressor, most of the impurities such as moisture, carbon dioxide, hydrocarbons, etc. are removed in the purification unit, and then the first supply air enters the main rectification device. The flow rate of the first supply air stream is generally greater than 200000Nm 3 H is the ratio of the total weight of the catalyst to the total weight of the catalyst. The main rectification unit comprises at least two columns thermally connected by a main condenser-evaporator at different pressures, an expander, a main heat exchanger, and optionally airSuperchargers, subcoolers, liquid pumps, etc. The liquid oxygen or gaseous oxygen product obtained in the main rectification device enters a krypton-poor mixture preparation unit (such as a krypton tower), and krypton-poor liquid with the content of 0.1-0.3% (Kr + Xe) is obtained after evaporation and concentration.
During the krypton concentration process, the hydrocarbon content also increases, and when the content is too high, it forms an explosive with the liquid oxygen, and therefore must be removed in a subsequent impurity removal unit. In this unit, first, hydrocarbons such as methane can be removed by catalytic reaction such as a catalyst, and moisture and carbon dioxide produced by the catalytic reaction can be further removed by adsorption using a molecular sieve such as 5A or 13X.
And concentrating the purified poor krypton liquid in a crude krypton and xenon preparation unit by adopting a rectification method or an adsorption method to prepare a krypton and xenon mixture (crude krypton) with higher purity. The adsorption method comprises a chromatographic separation method, wherein a gas mixture is added into a carrier gas, a chromatographic separation is carried out by a chromatographic column to obtain a plurality of binary mixtures (the carrier gas and a certain component), and then the binary mixtures are separated to obtain the required gas product. The rectification method is that the poor krypton liquid is further concentrated in the krypton-II tower, and then fed into the krypton-III tower for intermittent rectification, so that krypton and xenon are separated, and finally krypton and xenon with the purity respectively higher than 99% are obtained and output as industrial products.
The first air rectification apparatus of the present invention may optionally further comprise a pure krypton, xenon production unit when higher purity (> 99.9%) of krypton or xenon is desired to be produced. In the unit, impurities such as oxygen, nitrogen, hydrogen, hydrocarbon and the like in industrial krypton and xenon are removed through catalytic reaction and adsorption.
In the embodiment of fig. 1, in order to increase the production of krypton, xenon in the first air rectification plant, a make-up gas stream containing the preliminary enrichment of krypton, xenon is fed before the inlet end of the main air compressor, as long as the ratio of the flow rate of this make-up gas stream to the flow rate of the first feed air stream is not greater than 1%, preferably not greater than 0.5%, no changes need to be made in the equipment and piping, operating parameters, etc. of the first air rectification plant. The make-up gas stream originates from one or more second air rectification plants featuring at least one condensing evaporator which generates condensing evaporator drains continuously or intermittently in daily operation or in case of maintenance shutdowns or the like. The continuous liquid discharge refers to the continuous discharge of liquid oxygen in the condensation evaporator; the intermittent liquid discharge refers to the discontinuous liquid discharge in a mode of discharging liquid oxygen in a condensing evaporator at regular time and the like. In contrast to the prior art, in which such discharges are reheated and discharged to the atmosphere, in fig. 1, these discharges are transported via pipelines or collected via a tanker to the first air rectification plant, vaporized in a vaporizer, fed as a make-up gas stream to the front end of the main air compressor of the first air rectification plant, mixed with the original first supply air stream, and separated in the first air rectification plant to produce purified krypton and/or xenon.
The second air rectification apparatus in the present invention is an air rectification apparatus which does not include any krypton or xenon extraction device and can be used for separating oxygen, nitrogen, argon, and the like, and examples thereof include a nitrogen generator and a two-column air separation plant.
The condensing evaporator, also known as the reboiler, condenser or evaporator, of the second air rectification apparatus is primarily operative to exchange heat between a higher pressure gas (e.g., nitrogen-rich gas) and a lower pressure liquid (e.g., oxygen-rich liquid) to condense the former to produce a reflux and vaporize the latter to form an ascending vapor. In operation, hydrocarbons in the feed air dissolve in the liquid oxygen and accumulate in the condenser evaporator and even condense out, creating a risk of explosion. When the second air rectification device produces the liquid oxygen product, a part of dangerous impurities are continuously discharged from the condensation evaporator along with the liquid oxygen product; however, when the second air distillation plant produces only nitrogen or oxygen products, a certain amount of liquid oxygen must be discharged in a continuous or intermittent manner for safety and explosion protection, since this not only discharges a portion of solid hazardous impurities, but also keeps the liquid oxygen in a flowing condition at all times, which is the condensate evaporator discharge of the present invention.
If the shutdown time of the device is long due to overhaul, liquid oxygen and liquid air in the device need to be discharged, and the liquid oxygen and the liquid air in the device do not need to be naturally evaporated so as to avoid concentration and precipitation of hydrocarbons containing acetylene, and the like, which is the liquid discharge of the condensation evaporator.
Fig. 2 shows one possibility of a second air rectification device, namely a nitrogen generator. In the simplified flow scheme of fig. 2, compressed, cooled, purified air is fed to the bottom of a single column 3 after indirect heat exchange with the return gas in a main heat exchanger 2. In a rectification section 9 of the single tower 3, oxygen and nitrogen are separated, oxygen-enriched liquid air 7 is generated at the bottom of the single tower 3, pure nitrogen is generated at the upper part of the rectification section 9, and a part 10 of the pure nitrogen is output as a product after being reheated in the subcooler 4 and the main heat exchanger 2 respectively; the other portion 8 enters the main condensing evaporator 5 through a pipe. The oxygen-enriched liquid air 7 is subcooled in the subcooler 4 and then is introduced into the main condensation evaporator 5 to indirectly exchange heat with the pure nitrogen 8, the oxygen-enriched liquid air 7 is partially vaporized, and the pure nitrogen 8 is condensed and then is conveyed back to the rectification section 9 to be used as reflux liquid. The waste nitrogen 11 (the content of nitrogen is more than 95%) generated at the top of the single tower 3 is partially reheated in the subcooler 4 and the main heat exchanger 2 respectively, then is expanded and refrigerated in the expander 6, and passes through the subcooler 4 and the main heat exchanger 2 respectively again, thereby providing the refrigeration required by the operation of the rectifying device. Since the nitrogen generator of fig. 2 only produces nitrogen product, impurities, hydrocarbons, etc. that enter the apparatus with air can accumulate in the liquid oxygen in the main condenser-evaporator 5, with a significant safety risk if not discharged in time. Therefore, the discharged liquid of the condensing evaporator can be continuously discharged in operation, and the local concentration, separation and accumulation of dangerous impurities in the condensing evaporator are avoided. For example, the composition of the condensate evaporator effluent contains roughly 60% oxygen, 39% nitrogen, around 100ppm hydrocarbons and tens of ppm krypton and xenon. In addition to the simplified nitrogen generator apparatus and process shown in fig. 2, those skilled in the art will appreciate that all other types of nitrogen generators are consistent with the spirit of the present invention.
Fig. 3 shows another possibility of the second air rectification unit, namely the low-pressure process for producing oxygen by external compression. As can be seen from fig. 3, the compressed, cooled and purified air is divided into two parts, the first part 101 is indirectly heat exchanged with the return gas in the main heat exchanger 201 and then fed to the bottom of the lower column 202; the second part 102 is compressed by the booster end 203 of the expansion booster and then is introduced into the main heat exchanger 201, and the second part is introduced into the expansion end 204 of the expansion booster after being extracted in the middle part, expanded and cooled, and then introduced into the middle lower part of the upper tower 205. The lower column 202 and the upper column 205 are in thermal communication via the main condensing evaporator 207, and the operating pressure of the lower column 202 is higher than that of the upper column 205. The lower column 202 separates the air stream 101 after rectification into a bottom oxygen-rich liquid air 103 and a top pure nitrogen gas 104, 105. A part 104 of the pure nitrogen is supercooled in a supercooler 206 and throttled to obtain liquid nitrogen as a product for output; another portion 105 is compressed to a suitable pressure by nitrogen compressor 207 after being reheated in main heat exchanger 201 as a nitrogen product output. The oxygen-enriched liquid air 103 is subcooled by a cooler 206 and is input to the middle upper part of the upper tower after being throttled. The nitrogen-lean gas 106 withdrawn from the upper middle section of the lower column is also subcooled in subcooler 206 and throttled and sent to the upper section of upper column 205 as reflux. The nitrogen purge 107 is withdrawn at the top of the upper column 205, passed through a condenser 206 and main heat exchanger 201 respectively for reheating and then vented to the atmosphere or to a regeneration or cold source of a water cooling column used in a purification plant. This unit does not produce liquid oxygen, but instead draws oxygen 108 at the bottom of the lower column, which is reheated in main heat exchanger 201 and compressed to the pressure required by the customer using a suitable oxygen compressor 208. Pure nitrogen gas, which is not shown in fig. 3 and includes a lower column, enters the main condensing evaporator 207, liquid nitrogen is obtained by condensation as a reflux liquid of the lower column and liquid oxygen obtained by the upper column is partially vaporized in the main condensing evaporator 207. Since this plant does not produce liquid oxygen product, the hazardous impurities accumulated in the main condenser-evaporator 207 need to be vented through a continuous condenser-evaporator vent, which typically contains several hundred ppm hydrocarbons, about 40-70 ppm krypton and about 10-40 ppm xenon.
Example 1
The first air distillation device for preparing krypton/xenon products is 3000 tons of oxygen produced per day, and the air feeding amount is 440000Nm 3 The daily yield of krypton is 6.89Nm under the normal operation condition of the air rectification device 3 Daily yield of xenon of 0.75Nm 3 。
The second air rectification device is selected as shown in figure 2A nitrogen making machine. For nitrogen the yield was 60000Nm 3 For the/h nitrogen generator, the flow rate of the condensed evaporator discharged liquid after vaporization is 200Nm in normal operation 3 A concentration of about 100ppm hydrocarbons, about 37ppm krypton and about 30ppm xenon. Because the ratio of the flow rate to the air feeding amount of the first air rectifying device is only 0.045% and is far less than 1% of the flow path and equipment of the first air rectifying device which may need to be changed, when the liquid discharged by the condensation evaporator of the vaporized nitrogen making machine is directly input into the first air rectifying device at the front end of the main air compressor, the daily yield of krypton is 8.07Nm 3 Daily yield of xenon of 0.94Nm 3 Corresponding to 17% and 24% yield improvement, respectively. If the condensate evaporator drains of a plurality of sets of second air rectification devices are mixed with the feed air of the first air rectification device, the yield of krypton/xenon in the latter can be further improved.
Example 2
The first air distillation device for preparing krypton/xenon products is 3000 tons of oxygen produced per day, and the air feeding amount is 440000Nm 3 The daily yield of krypton is 6.89Nm under the normal operation condition of the air rectification device 3 Daily yield of xenon of 0.75Nm 3 。
The second air distillation device is selected from an oxygen generation device adopting an external compression flow path as shown in figure 3. For a 2000 ton per day oxygen plant, the flow of the condenser evaporator bleed after vaporization was 580Nm during normal operation 3 A concentration of about several hundred ppm hydrocarbons, about 57ppm krypton and about 30ppm xenon. Because the ratio of the flow rate to the air feeding quantity of the first air rectification device is only 0.13 percent and is far less than 1 percent of the flow path and equipment which possibly need to be changed of the first air rectification device, when the vaporized liquid discharged from the condensation evaporator of the device is directly input into the first air rectification device at the front end of the main air compressor, the daily yield of krypton is 10.11Nm 3 Daily yield of xenon is 1.25Nm 3 This corresponds to a yield increase of 46% and 66%, respectively. If the liquid discharge of the condensation evaporator of a plurality of sets of second air rectification devices is mixed with the feed air of the first air rectification device, one air can be fedThe yield of krypton/xenon is increased. For example, if the nitrogen generator of the first embodiment and the condenser-evaporator discharge of the oxygen production plant of the second embodiment are simultaneously fed to the first air rectification plant, a daily yield of krypton of 11.29 Nm/l can be obtained 3 Daily yield of xenon is 1.44Nm 3 This corresponds to 63% and 91% yield improvement.
The embodiments described in the specification are only preferred embodiments of the present invention, and the above embodiments are only used to illustrate the technical solutions of the present invention and not to limit the present invention. Those skilled in the art can obtain technical solutions through logical analysis, reasoning or limited experiments according to the concepts of the present invention, and all such technical solutions are within the scope of the present invention.

Claims (10)

1. A method for increasing the yield of krypton/xenon in an air distillation apparatus, comprising:
a) Providing a first feed air stream and a first air rectification device, wherein the first feed air stream is separated in the first air rectification device to obtain krypton/xenon product,
b) Providing at least one set of second air rectification device with a condensation evaporator, wherein the condensation evaporator of the second air rectification device generates condensation evaporator drainage liquid which is oxygen-enriched liquid enriched in krypton/xenon;
c) Collecting and vaporizing the condensate evaporator drain liquid, mixing the vaporized condensate evaporator drain liquid with a first supply air flow, and separating in a first air rectification device to obtain a krypton/xenon product;
wherein the flow ratio of the vaporized condenser-evaporator drain to the first feed air stream is no greater than 1%.
2. The method of claim 1 wherein the flow ratio of the vaporized condensing evaporator drain to the first supply air stream is no greater than 0.5%.
3. The method of claim 1 wherein the first air rectification device comprises a main air compressor and the vaporized condensate evaporator drain is mixed with the first feed air stream at an inlet end of the main air compressor.
4. The method of claim 1, wherein the second air rectification device comprises an air rectification device that produces only nitrogen.
5. The method as claimed in claim 1, wherein said second air distillation apparatus comprises an air distillation apparatus for producing an oxygen gas product by external compression.
6. The method of claim 1, wherein the condensing evaporator draw-down occurs during routine operation and/or during servicing and emptying of the second air distillation unit.
7. The method of claim 1 wherein said second air distillation apparatus comprises a plurality of said second air distillation apparatuses.
8. The method of claim 1 wherein the condensate evaporator drain from the second air rectification plant is transported to the first air rectification plant by piping or tanker truck.
9. The method of claim 1, wherein the first air rectification device comprises a main air separation unit, a depleted krypton extraction unit, an impurity removal unit, a crude krypton production unit, a pure krypton and crude xenon production unit, and a crude xenon purification unit.
10. The method as claimed in claim 1, characterized in that the condensate evaporator discharges from 0.1 to 0.2% of the total air processed by the second air rectification device.
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Family Cites Families (18)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2051576A (en) * 1936-04-06 1936-08-18 Air Reduction Recovery of krypton and xenon
DE1667639A1 (en) * 1968-03-15 1971-07-08 Messer Griesheim Gmbh Method for obtaining a krypton-xenon mixture from air
JPH0665948B2 (en) * 1985-07-26 1994-08-24 日本酸素株式会社 Method for concentrating krypton and xenon in an air separation device
DE19708780A1 (en) * 1997-03-04 1998-09-10 Linde Ag Process for krypton and xenon extraction
US6314757B1 (en) * 2000-08-25 2001-11-13 Prakair Technology, Inc. Cryogenic rectification system for processing atmospheric fluids
US6735980B2 (en) * 2002-01-04 2004-05-18 Air Products And Chemicals, Inc. Recovery of krypton and xenon
DE10228111A1 (en) * 2002-06-24 2004-01-15 Linde Ag Air separation process and plant with mixing column and krypton-xenon extraction
FR2847568B1 (en) * 2002-11-25 2005-02-11 Air Liquide PROCESS AND PLANT FOR PRODUCING KRYPTON / XENON MIXTURE FROM AIR
US6694775B1 (en) * 2002-12-12 2004-02-24 Air Products And Chemicals, Inc. Process and apparatus for the recovery of krypton and/or xenon
FR2930629B1 (en) * 2008-04-23 2010-05-07 Air Liquide APPARATUS AND METHOD FOR AIR SEPARATION BY CRYOGENIC DISTILLATION
CN101723338B (en) * 2009-11-12 2013-03-13 上海启元科技发展有限公司 Method for extracting krypton-xenon from liquid oxygen
FR2990500A1 (en) * 2012-05-11 2013-11-15 Air Liquide METHOD AND APPARATUS FOR AIR SEPARATION BY CRYOGENIC DISTILLATION
FR3020867B1 (en) * 2014-05-07 2019-03-29 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude METHOD AND APPARATUS FOR AIR SEPARATION BY CRYOGENIC DISTILLATION FOR THE PRODUCTION OF A MIXTURE OF KRYPTON AND XENON
US10995982B2 (en) * 2016-01-11 2021-05-04 Praxair Technology, Inc. System and method for rare gas recovery
CN105865148B (en) * 2016-04-01 2019-06-04 上海启元空分技术发展股份有限公司 A method of efficiently producing high pure oxygen and High Purity Nitrogen
CN108302899A (en) * 2018-03-29 2018-07-20 浙江新锐空分设备有限公司 A kind of space division system and method extracting poor krypton xenon product using liquefied air
CN113654302B (en) * 2021-08-12 2023-02-24 乔治洛德方法研究和开发液化空气有限公司 Low-temperature air separation device and method
CN114195107A (en) * 2022-01-05 2022-03-18 郑州耀强化工产品有限公司 Device and process for concentrating krypton and xenon by liquid oxygen

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