CN111928573A - Argon preparation method - Google Patents

Argon preparation method Download PDF

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Publication number
CN111928573A
CN111928573A CN202010675940.6A CN202010675940A CN111928573A CN 111928573 A CN111928573 A CN 111928573A CN 202010675940 A CN202010675940 A CN 202010675940A CN 111928573 A CN111928573 A CN 111928573A
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CN
China
Prior art keywords
argon
gas
crude
column
nitrogen
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Pending
Application number
CN202010675940.6A
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Chinese (zh)
Inventor
李登桐
郭中山
黄斌
姜永
杨晓东
孟卫宁
田兴兵
岳峰
杜长银
王文龙
祁卫保
霍源
杨冰
高龙
伍超
杨健
马文超
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National Energy Group Ningxia Coal Industry Co Ltd
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National Energy Group Ningxia Coal Industry Co Ltd
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Application filed by National Energy Group Ningxia Coal Industry Co Ltd filed Critical National Energy Group Ningxia Coal Industry Co Ltd
Priority to CN202010675940.6A priority Critical patent/CN111928573A/en
Publication of CN111928573A publication Critical patent/CN111928573A/en
Pending legal-status Critical Current

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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
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04351—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
    • F25J3/04357—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen and comprising a gas work expansion loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • F25J3/0228—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 characterised by the separated product stream
    • F25J3/028—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 characterised by the separated product stream separation of noble gases
    • F25J3/0285—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 characterised by the separated product stream separation of noble gases of argon
    • 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
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B9/00—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point
    • F25B9/06—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point using expanders
    • 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
    • F25D—REFRIGERATORS; COLD ROOMS; ICE-BOXES; COOLING OR FREEZING APPARATUS NOT OTHERWISE PROVIDED FOR
    • F25D3/00—Devices using other cold materials; Devices using cold-storage bodies
    • F25D3/10—Devices using other cold materials; Devices using cold-storage bodies using liquefied gases, e.g. liquid 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
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04721—Producing pure argon, e.g. recovered from a crude argon column
    • F25J3/04727—Producing pure argon, e.g. recovered from a crude argon column using an auxiliary pure argon column for nitrogen rejection
    • 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
    • F25J5/00—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants
    • 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/58—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being argon or crude argon
    • 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/58—Processes or apparatus involving steps for recycling of process streams the recycled stream being argon or crude argon

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

The invention relates to the technical field of air separation and discloses an argon preparation method which comprises the step of evaporating crude argon at a low temperature by taking pressure nitrogen as a heat source. By increasing the ascending gas quantity, the argon yield and the argon extraction rate are effectively improved.

Description

Argon preparation method
Technical Field
The invention relates to an air separation technology, in particular to an argon preparation method.
Background
Currently, the argon preparation mainly comprises hydrogenation argon preparation and full-rectification argon preparation. The full-rectification argon preparation has the advantages of simple flow, convenient operation, safety, stability, high argon extraction rate and the like, and is widely applied. The full-rectification argon preparation is that oxygen-argon separation is carried out in a crude argon tower, and the oxygen content is directly obtained and is less than l x 10-6And performing argon-nitrogen separation on the crude argon in a fine argon tower to obtain a fine argon product with the purity of 99.999 percent. However, the existing air separation device is matched with an argon system to use argon fraction as the ascending gas of the crude argon tower, and the gas quantity is limited by the distillation working condition. The yield and extraction rate of argon are limited due to the small amount of gas rising and insufficient circulation rate. To is coming toIncreasing argon production and extraction rate, a new argon production method is urgently needed, by which argon production and extraction rate can be increased
Disclosure of Invention
The invention aims to overcome the problems that in the argon preparation tower in the prior art, the ascending gas quantity is small, the circulation multiplying power is insufficient, and the argon yield and the extraction rate are limited, and provides an argon preparation method which can provide enough ascending gas to improve the argon yield and the argon extraction rate.
In order to achieve the above object, the present invention provides an argon production method including low-temperature evaporation of crude argon gas using pressurized nitrogen gas as a heat source.
Further, the argon preparation method comprises the step of evaporating the first crude argon in the crude argon column through a first evaporator at the bottom of the crude argon column by using the pressure nitrogen as a heat source.
Further, the argon production method includes condensing a first ascending gas ascending after being evaporated by the first evaporator in an upper portion of the crude argon column by a first condenser.
Further, the argon preparation method comprises the step of sending part of second crude argon gas subjected to primary purification of the crude argon tower into the fine argon tower.
Further, the argon preparation method comprises the step of evaporating the second crude argon through a second evaporator at the bottom of the fine argon tower by using the pressure nitrogen as a heat source.
Further, the argon production method comprises the step of condensing second ascending gas ascending after being evaporated by the first condenser at the upper part of the fine argon column through a second condenser.
Further, the argon production method comprises the step of conveying feed gas conveyed from the air separation unit to the crude argon column through a second compression device to be used as the crude argon.
Further, the argon preparation method comprises the step of exchanging heat between the pressure nitrogen and the feed gas through a heat exchanger to reduce the temperature of the feed gas and the pressure nitrogen to a set temperature.
Further, the argon making method comprises the step of providing cold energy for the heat exchanger through an expander or liquid nitrogen.
Further, the argon production method comprises the step of providing the set pressure for the pressure nitrogen through the first compression device.
Further, the argon production method comprises refrigerating the heat exchanger, the crude argon column and the fine argon column through a cold box.
According to the technical scheme, the pressure nitrogen is used as a heat source to evaporate the crude argon at low temperature. By increasing the ascending gas quantity, the argon yield and the argon extraction rate are effectively improved.
Drawings
FIG. 1 is a schematic view of an argon production system in accordance with one embodiment of the present invention.
Description of the reference numerals
1-a crude argon column; 11-a first evaporator; 111-a first inlet; 112-a first outlet; 12-a first condenser; 121-a second inlet; 122-a second outlet; 13-a first chamber; 14-a second chamber; 16-a first diaphragm assembly; 15-a first opening; 2-a fine argon column; 21-a second evaporator; 211-a third inlet; 212-a third outlet; 22-a second condenser; 221-a fourth inlet; 222-a fourth outlet; 23-a third chamber; 24-a fourth chamber; 26-a second baffle assembly; g1 — first conduit; g 2-a second conduit; g 3-third conduit; g 4-fourth conduit; g 5-fifth conduit; g 6-sixth conduit; g 7-seventh conduit; 3-a pressure and temperature regulating device; 31-a first compression device; 32-a heat exchanger; 33-second compression device.
Detailed Description
The following detailed description of embodiments of the invention refers to the accompanying drawings. In the present invention, the use of directional terms such as "upper, lower, left, right" generally means the position where it is actually used, unless otherwise specified. "inner and outer" refer to the inner and outer contours relative to the object.
The present invention will be described in detail below with reference to the accompanying drawings in conjunction with embodiments.
In order to achieve the above object, the present invention provides an argon production method, as shown in fig. 1, which includes cryogenically evaporating crude argon gas using pressurized nitrogen gas as a heat source. The oxygen, the nitrogen and the argon are respectively separated by utilizing the difference of the evaporation temperature of the nitrogen, the oxygen and the argon. Preferably, the argon preparation method comprises the step of evaporating the first crude argon in the crude argon column through a first evaporator at the bottom of the crude argon column by using the pressure nitrogen as a heat source. In this case, the first crude argon gas whose pressure nitrogen gas is in a liquid state is heated by using the fact that the evaporation point of argon gas is lower than that of oxygen gas under the same pressure and temperature conditions, and the argon gas is gasified and separated from the liquid oxygen gas.
Preferably, the argon production method includes condensing a first ascending gas ascending after being evaporated by the first evaporator at an upper portion of the crude argon column by a first condenser. The first lift gas is mainly a mixture of nitrogen and argon, and under the same temperature and pressure, the nitrogen and the argon are evaporated, and a very small part of oxygen remained in the first lift gas is liquefied, so that the oxygen can be further separated. The pressure nitrogen is refrigerated by first crude argon from the first evaporator and then rises to the upper part of the crude argon tower from the first evaporator along the pipeline to provide a cold source for the first condenser, the temperature of the first rising gas is reduced under the condensation effect of the nitrogen, one part of the first rising gas is discharged from the crude argon tower to enter the next link, and the other part of the first rising gas enters the crude argon tower for circulation.
Preferably, the argon production method comprises sending part of the second crude argon subjected to the primary purification of the crude argon column to the fine argon column. The argon and the nitrogen are separated in the fine argon tower and purified again, so that the argon with higher purity can be obtained.
Preferably, the argon preparation method comprises the step of evaporating the second crude argon through a second evaporator at the bottom of the fine argon column by using the pressure nitrogen as a heat source. Utilize the evaporating temperature difference of nitrogen gas, argon gas, the pressure nitrogen gas that comes from first compression equipment through the heat exchanger heats the second crude argon gas in the smart argon tower, and the second crude argon gas is heated low temperature evaporation and is formed the second lift gas that uses nitrogen gas as the owner, and argon gas becomes liquid argon deposit in the bottom of smart argon tower.
Preferably, the argon production method comprises a condensing operation of a second ascending gas ascending after being evaporated by the first condenser at an upper portion of the fine argon column by a second condenser. The second ascending gas is cooled by the nitrogen conveyed from the second evaporator, and the nitrogen and the argon in the second ascending gas are further separated: the separated liquid nitrogen flows into the bottom of the fine argon column, and the separated nitrogen is directly discharged when the separated nitrogen is accumulated to a set degree. Discharging nitrogen which is used for providing a cold source for the second condenser from the second evaporator, and emptying the nitrogen after the nitrogen is heated by the second ascending gas, so that the argon with high purity is obtained
Preferably, the argon production method comprises conveying feed gas conveyed from the air separation unit to the crude argon column through the second compression device as the crude argon. Through utilizing the second compression to pressurize first crude argon gas, can make the crude argon gas that produces from each air separation plant like this can both adapt to the requirement of crude argon tower, like this, to a plurality of air separation plants, all can utilize this crude argon tower to very big saving manufacturing cost.
Preferably, the argon production method comprises the step of reducing the temperature of the feed gas and the pressure nitrogen to a set temperature by exchanging heat between the pressure nitrogen and the feed gas through a heat exchanger. So that the pressure of the nitrogen and the raw material gas are both reduced to the set temperature, thereby carrying out low-temperature evaporation.
Preferably, the argon production method comprises providing cold to the heat exchanger through an expander or liquid nitrogen. The nitrogen is continuously discharged along with the argon extraction work, so the pressure of the nitrogen is continuously reduced, and in the crude argon tower, the nitrogen provides a cold source for the first condenser and absorbs heat, so the temperature is increased; the nitrogen after the temperature increase is discharged from the top of the crude argon column and then recycled. Therefore, the system needs to be supplemented with cold and nitrogen.
Preferably, the argon production method comprises providing the set pressure to the pressure nitrogen gas through a first compression device. By pressurizing the nitrogen, more nitrogen can be contained per unit volume.
Preferably, the argon production method comprises refrigerating the heat exchanger, the crude argon column and the fine argon column through a cold box. Because the extraction of argon is carried out in a low-temperature environment, the heat exchanger, the crude argon column and the fine argon column are arranged in the cold box by arranging the cold box, so that the heat exchanger, the crude argon column and the fine argon column can be kept in a set temperature range.
In the embodiment shown in fig. 1, an argon production system comprises a crude argon column 1, a first evaporator 11 disposed inside a shell of the crude argon column 1, and a first condenser 12 disposed inside a column body of the crude argon column 1; the first condenser 12 is located above the first evaporator 11; the method comprises the steps that a feeding hole and a discharging hole are formed in a tower body of a crude argon tower 1, the feeding hole is arranged below the discharging hole, crude argon enters the crude argon tower 1 from the feeding hole and is then purified and then discharged to a designated place from the discharging hole, nitrogen is used as a heat source in a first evaporator 11, separation of oxygen and argon is mainly carried out in the crude argon tower 1, the first evaporator 11 which takes pressure nitrogen as the heat source is arranged at the bottom of the crude argon tower 1, nitrogen with set temperature and pressure is introduced into the first evaporator 11 from a first inlet 111 of the first evaporator 11 to carry out low-temperature evaporation on the first crude argon in the crude argon tower 1 by utilizing the difference of evaporation points of the nitrogen, the argon and the oxygen, and cooled nitrogen flows out of the first evaporator 11 from a first outlet 112; in this way, the ascending gas quantity in the crude argon column 1 is increased, and the circulation multiplying power is increased.
The crude argon column 1 further comprises a first baffle assembly 16; the first baffle plate assembly 16 divides the interior of the tower body of the crude argon tower 1 into a first chamber 13 and a second chamber 14 which are arranged from bottom to top; separating the first chamber 13 from the second chamber 14 by means of a first baffle assembly 16, in preparation for the cyclic condensation of argon between the first chamber 13 and the second chamber 14, the first condenser 12 being arranged in the second chamber 14; the first evaporator 11 is disposed at a lower portion of the first chamber 13. First crude argon gas gets into in crude argon tower 1 from the feed inlet of crude argon tower 1, in crude argon tower 1, argon gas becomes gaseous back and liquid oxygen separation, and liquid oxygen deposit is in the bottom of first cavity 13, and argon gas rises from first cavity 13, forms first upwelling, through the heating of first evaporimeter 11, the ascending volume grow of first upwelling in the crude argon tower 1 to be favorable to preparing of argon gas.
The first evaporator 11 comprises a first inlet 111 for connecting a nitrogen gas source and a first outlet 112 for discharging nitrogen gas; the argon making system comprises a first pipe g1 communicating the first outlet 112 and the second chamber 14 to send the nitrogen gas discharged from the first outlet 112 into the second chamber 14 as a cold source of the first condenser 12; the nitrogen enters the first evaporator 11 from the first inlet 111 to heat the first crude argon gas containing oxygen and argon, meanwhile, the nitrogen is cooled by the first crude argon gas itself, and the nitrogen with the cooled temperature reduced is discharged from the first outlet 112 and enters the second chamber 14 through the first pipe g1 to provide a cold source for the first condenser 12; the crude argon column 1 comprises a first opening 15 formed on the top wall of the second chamber 14 for discharging the nitrogen gas heated by the first condenser 12 outside the column 1; the heated nitrogen gas is discharged from the crude argon column 1 through the first opening 15, so that the nitrogen gas continuously enters the first evaporator 11 from the nitrogen gas source to warm and evaporate the crude argon in the first chamber 13. The nitrogen gas exiting the crude argon column 1 can be recycled.
The first condenser 12 comprises a second inlet 121 and a second outlet 122 for the argon; the argon production system comprises a third conduit g3 and a second conduit g2 communicating the first chamber 13 and the first condenser 12; the second pipe g2 communicates the first chamber 13 with the second inlet 121, and the third pipe g3 communicates the first chamber 13 with the second outlet 122 to enable argon gas to circulate between the first chamber 13 and the first condenser 12. This prevents the first condenser 12 from being clogged. Argon gas from the first chamber 13 enters the first condenser 12 through the second inlet 121 through the second pipeline g2, and then a part of argon gas returns to the first chamber 13 through the second outlet 122 to form an argon cycle, at this time, the argon gas flows through the first condenser 12, and nitrogen gas flows out of the first condenser 12, because the volume of the second chamber 14 is large, and it is easier to expand the volume of the second chamber 14, more nitrogen gas can be contained in the second chamber 14 as a cold source, the condensation effect is strong, the temperature difference is large, and the extraction rate and the extraction amount of argon can be improved.
The argon production system further comprises a fourth conduit g4 passing through the column wall of the crude argon column 1 and communicating with the second outlet 122 to discharge a portion of the second crude argon to a designated location. During the argon extraction, the first crude argon enters the first chamber 13, most of the oxygen in the first crude argon is separated in the first ascending gas which ascends after being heated by the first evaporator 11, the first ascending gas enters the first condenser 12 from the upper part of the first chamber 13 through the second pipeline g2 to separate oxygen again, a part of the condensed gas, i.e. the second crude argon gas, returns to the first chamber 13 from the third pipeline g3, which not only maintains the circulation of the first ascending gas between the first condenser 12 and the first chamber 13 to effectively prevent blockage in the first condenser 12, but also can deposit a part of the separated oxygen gas again to the bottom of the first chamber 13 to complete oxygen gas separation again, and another part of the condensed second crude argon gas is sent to a designated place through the fourth pipeline g4, wherein the crude argon gas, i.e. the second crude argon gas, at this time mainly comprises nitrogen gas and argon gas.
The argon production system comprises a fine argon column 2, the fine argon column 2 comprising a second baffle assembly 26; the second partition plate assembly 26 partitions the interior of the column body of the fine argon column 2 into a third chamber 23 and a fourth chamber 24 which are distributed from bottom to top. In the fine argon column 2, the separation of argon and nitrogen is mainly carried out. The second crude argon gas discharged from the second outlet 122 and separated from oxygen by the crude argon column 1 is introduced into the fine argon column 2 through the fourth pipe g4 to be purified again. In the fine argon column 2, the third chamber 23 and the fourth chamber 24 are separated by the second partition plate assembly 26, thereby preparing for the cyclic condensation of argon gas between the third chamber 23 and the fourth chamber 24.
The argon making system comprises a second condenser 22 arranged in the fourth chamber 24 and a second evaporator 21 arranged in the lower part of the third chamber 23; the fourth duct g4 communicates the second outlet 122 with the third chamber 23. The second evaporator 21 serves to increase the amount of the second lift gas in the argon purification column 2. The second condenser 22 condenses the second ascending gas ascending from the third chamber 23 using the cooled nitrogen gas discharged from the second evaporator 21 as a cold source, and further purifies the argon gas.
The second evaporator 21 includes a third inlet 211 and a third outlet 212 for the ingress and egress of nitrogen supplied from the nitrogen source; the second condenser 22 comprises a fourth inlet 221 and a fourth outlet 222; the third inlet 211 is communicated with a nitrogen source which is used as a heat source of the second evaporator 21; the argon making system further comprises a fifth pipe g5 connecting the third outlet 212 and the fourth inlet 221 to provide a cold source for the second condenser 22 using the nitrogen discharged from the second evaporator 21; the fourth outlet 222 is directly connected to the atmosphere to evacuate the nitrogen gas heated by the second condenser 22.
Because the separation of argon and nitrogen is carried out in the fine argon column 2, the argon with higher purity is obtained after cooling, and the argon is gradually collected at the bottom of the third chamber 23 along with the production and then is discharged to a storage tank through a set pipeline for storage.
The argon production system comprises a sixth conduit g6 leading from the third chamber 23 to the upper part of the fourth chamber 24; a seventh duct g7 leading from the lower part of the fourth chamber 24 to the third chamber 23; so as to enable the circulation of argon between the third chamber 23 and said fourth chamber 24. Thus, the nitrogen gas and the argon gas can be further separated while the second condenser 22 is prevented from being clogged. The separated nitrogen is directly evacuated.
The bottom wall of the third chamber 23 is provided with a discharge port for sending the liquid argon to a designated place. As shown in fig. 1, since the separation of argon gas and nitrogen gas is mainly performed in the fine argon column 2, and the argon gas becomes liquid after condensation and is deposited on the lower portion of the fine argon column 2, the liquid argon is introduced into the storage tank through the discharge port provided on the bottom wall of the third chamber 23 to be stored.
The argon preparation device comprises a pressure temperature adjusting device 3 and a cold box, and the crude argon tower 1 and the fine argon tower 2 are arranged in the cold box. The crude argon column 1 and the fine argon column 2 can be maintained in a low temperature environment by means of a cold box.
The pressure and temperature adjusting device 3 further comprises a heat exchanger 32 arranged in the cold box and a first compression device 31 arranged outside the cold box; by arranging the heat exchanger 32 in the cold box, the heat exchanger 32 is kept in a low-temperature state, so that nitrogen can be subjected to heat exchange from normal temperature to low temperature; the nitrogen is pressurized through the first compression equipment 31, so that the pressure requirement of the system on the nitrogen is met; the outlet line of the first compression device 31 is respectively communicated with the first evaporator 11 and the second evaporator 21 after passing through the heat exchanger 32, so that the first evaporator 11 and the second evaporator 21 are simultaneously supplied with pressure nitrogen through one compressor, thereby facilitating operation and saving cost. Nitrogen gas after compressing through first compression equipment 31 passes through heat exchanger 32 heat transfer, reaches lower temperature, according to the difference of the gasification temperature of nitrogen gas, oxygen, argon gas, improves the ascending volume of argon gas in crude argon tower 1, improves the ascending tolerance of nitrogen gas in smart argon tower 2, and then improves the extraction capacity of argon.
The pressure and temperature adjusting device 3 comprises a second compression device 33 which is arranged outside the cold box and is used for connecting an air separation device, so that crude argon discharged from the air separation device is compressed by the second compression device 33 and then matched with the crude argon tower 1; when different air separation plant insert this system argon device, only need insert second compression equipment 33 in air separation plant's exit can realize, just so can satisfy one set of system argon device and can satisfy many sets of air separation plant simultaneously to need not the entire system all to park when overhauing air separation plant. The production efficiency is effectively improved. The heat exchanger 32 is provided between the second compression device 33 and the crude argon column 1, so that the crude argon discharged from the second compression device 33 is changed into low-temperature crude argon after heat exchange by the heat exchanger 32, and the low-temperature crude argon is sent into the crude argon column 1 for low-temperature evaporation.
The nitrogen discharged from the first opening 15 is pressurized again by the first compression device 31, and enters the first evaporator 11 and the second evaporator 21 again for recycling after heat exchange is performed by the heat exchanger 32.
The argon making device also comprises a liquid argon source or an expander, and cold energy is supplemented for the heat exchanger 32 through the liquid argon source or the expander, because along with the production, if the cold energy is not supplemented, the temperature of the heat exchanger 32 is higher and higher, and the heat exchange function of the heat exchanger 32 is continuously reduced.
The preferred embodiments of the present invention have been described in detail above with reference to the accompanying drawings, but the present invention is not limited thereto. Within the scope of the technical idea of the invention, numerous simple modifications can be made to the technical solution of the invention, including combinations of the individual specific technical features in any suitable way. The invention is not described in detail in order to avoid unnecessary repetition. Such simple modifications and combinations should be considered within the scope of the present disclosure as well.

Claims (11)

1. The argon preparation method is characterized by comprising the step of evaporating crude argon at low temperature by using pressure nitrogen as a heat source.
2. The argon making method according to claim 1, comprising an operation of evaporating the first crude argon gas in the crude argon column by a first evaporator at the bottom of the crude argon column using the pressure nitrogen gas as a heat source.
3. The argon production method according to claim 2, comprising a condensing operation of a first ascending gas ascending after being evaporated by the first evaporator at an upper portion of the crude argon column by a first condenser.
4. Argon production method according to claim 3, characterized in that it comprises sending part of the second crude argon gas after the primary purification of the crude argon column (1) into a fine argon column.
5. The argon making method according to claim 4, comprising a second evaporator for evaporating the second crude argon gas at the bottom of the fine argon column by using the pressure nitrogen gas as a heat source.
6. The argon production method according to claim 5, comprising a second condenser for condensing a second ascending gas ascending after being evaporated by the first condenser in an upper portion of the fine argon column.
7. An argon production method according to claim 1, characterized in that it comprises feeding a raw material gas fed from an air separation unit to a crude argon column as the crude argon gas through a second compression device.
8. An argon production method according to claim 7, comprising reducing the temperature of the feed gas and the pressure nitrogen gas to a set temperature by heat exchanging the pressure nitrogen gas and the feed gas by a heat exchanger.
9. The argon production method according to claim 8, comprising providing cold to the heat exchanger through an expander or liquid nitrogen.
10. The argon production method according to claim 2, comprising providing the pressurized nitrogen gas with a set pressure by a first compression device.
11. An argon making method according to claim 8 or 9 wherein the heat exchanger, the crude argon column and the fine argon column are refrigerated by a cold box.
CN202010675940.6A 2020-07-14 2020-07-14 Argon preparation method Pending CN111928573A (en)

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Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0023838A1 (en) * 1979-08-06 1981-02-11 Air Products And Chemicals, Inc. Separation of gas mixtures
CN101968298A (en) * 2010-09-27 2011-02-09 开封空分集团有限公司 Separation and recovery device and method for argon and methane in synthetic ammonia relief gas
CN104406364A (en) * 2014-11-06 2015-03-11 杭州杭氧股份有限公司 Double-tower coupling type argon recovery and purifying equipment and argon recovery and purifying method
CN107606874A (en) * 2017-10-26 2018-01-19 上海联风能源科技有限公司 A kind of device of Full distillation purification recovery argon gas and its method for reclaiming argon gas
CN108731376A (en) * 2018-04-18 2018-11-02 衢州杭氧气体有限公司 A kind of argon gas production technology and its production line
CN110542279A (en) * 2019-09-10 2019-12-06 苏州市兴鲁空分设备科技发展有限公司 argon tail gas recovery and purification device containing methane and hydrocarbon

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0023838A1 (en) * 1979-08-06 1981-02-11 Air Products And Chemicals, Inc. Separation of gas mixtures
CN101968298A (en) * 2010-09-27 2011-02-09 开封空分集团有限公司 Separation and recovery device and method for argon and methane in synthetic ammonia relief gas
CN104406364A (en) * 2014-11-06 2015-03-11 杭州杭氧股份有限公司 Double-tower coupling type argon recovery and purifying equipment and argon recovery and purifying method
CN107606874A (en) * 2017-10-26 2018-01-19 上海联风能源科技有限公司 A kind of device of Full distillation purification recovery argon gas and its method for reclaiming argon gas
CN108731376A (en) * 2018-04-18 2018-11-02 衢州杭氧气体有限公司 A kind of argon gas production technology and its production line
CN110542279A (en) * 2019-09-10 2019-12-06 苏州市兴鲁空分设备科技发展有限公司 argon tail gas recovery and purification device containing methane and hydrocarbon

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Application publication date: 20201113