CN111023697A - Method and device for reducing liquid nitrogen usage amount in refining of krypton and xenon - Google Patents
Method and device for reducing liquid nitrogen usage amount in refining of krypton and xenon Download PDFInfo
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- CN111023697A CN111023697A CN201911143252.9A CN201911143252A CN111023697A CN 111023697 A CN111023697 A CN 111023697A CN 201911143252 A CN201911143252 A CN 201911143252A CN 111023697 A CN111023697 A CN 111023697A
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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
- F25J3/0228—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
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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
- F25J3/04278—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using external refrigeration units, e.g. closed mechanical or regenerative refrigeration units
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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
- F25J3/04254—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using the cold stored in external cryogenic fluids
- F25J3/0426—The cryogenic component does not participate in the fractionation
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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
- F25J3/04642—Recovering noble gases from air
- F25J3/04745—Krypton and/or Xenon
- F25J3/04751—Producing pure krypton and/or xenon recovered from a crude krypton/xenon mixture
- F25J3/04757—Producing pure krypton and/or xenon recovered from a crude krypton/xenon mixture using a hybrid system, e.g. using adsorption, permeation or catalytic reaction
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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
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/82—Processes or apparatus using other separation and/or other processing means using a reactor with combustion or catalytic reaction
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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
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/42—Nitrogen
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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
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/34—Krypton
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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
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/36—Xenon
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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
- F25J2270/00—Refrigeration techniques used
- F25J2270/42—Quasi-closed internal or closed external nitrogen refrigeration cycle
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- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
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- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
The invention relates to a method for reducing the usage amount of liquid nitrogen in krypton-xenon refining, wherein a cold source of a condensation evaporator in a fractionating tower is low-temperature gas obtained by mixing the liquid nitrogen and nitrogen, and the low-temperature nitrogen and normal-temperature nitrogen in the cold source of the condensation evaporator of each rectifying tower are mixed in different proportions according to different operating temperatures of each rectifying tower in the fractionating tower. Still relate to a device that reduces liquid nitrogen use amount in krypton xenon refines, include: a fractionation column for krypton-xenon purification and a main heat exchanger for collecting and reheating nitrogen from each condensing evaporator, further comprising: and the circulating compressor is used for receiving the reheated nitrogen and increasing the pressure. According to the invention, the high-temperature nitrogen is extracted from the middle part of the main heat exchanger to serve as the heat flow for temperature regulation, so that the cold energy of liquid nitrogen is recovered, and the consumption of the liquid nitrogen refined by krypton and xenon can be greatly reduced.
Description
Technical Field
The invention relates to a gas separation method, in particular to a method and a device for reducing the use amount of liquid nitrogen in refining krypton-xenon.
Background
The atmospheric krypton and xenon contents are about 1.138X 10 respectively-6And 0.0857 × 10-6After trace krypton and xenon enter a low-temperature rectifying tower of an air separation device along with air, high-boiling-point components of krypton, xenon, hydrocarbon (mainly methane) and fluoride are accumulated in liquid oxygen of a low-pressure tower, and the liquid oxygen of the low-pressure tower is sent to a krypton additional rectifying tower (commonly called a poor krypton tower). The krypton-xenon-poor concentrate with Kr + Xe content of 0.2-0.3% can be obtained, wherein the methane content is about 0.3-0.4%. The methane content in oxygen is too high (generally not more than 0.5% CH)4) It is extremely dangerous that it is only possible to continue increasing the concentration of krypton and xenon in the liquid oxygen after the methane in the depleted krypton-xenon concentrate has been previously removed, in the known method the depleted krypton-xenon concentrate is first fedThe pressure is increased to 5.5MPa, the gas is vaporized, and the gas enters a methane purification device after being decompressed to 1.0 MPa. The methane purification device removes methane (the content of residual methane can be lower than 1 multiplied by 10) after oxygen and methane are subjected to chemical reaction at 480-500 ℃ through a palladium catalyst-6) Then, the chemical reaction products of carbon dioxide and water are removed by molecular sieve adsorption. And feeding the feed gas without methane into a first-stage rectifying tower to obtain a krypton-xenon mixture.
The general refining equipment uses the krypton-xenon mixture as a raw material, uses a mixed gas of nitrogen and liquid nitrogen as a cold source, separates krypton and xenon in a multi-stage rectification mode, and further purifies krypton and xenon. The nitrogen used by the refining equipment directly enters the cold box without a precooling process, and the amount of the liquid nitrogen used correspondingly is larger.
Accordingly, those skilled in the art have endeavored to develop methods for refining krypton and xenon, and more specifically, methods for reducing the amount of liquid nitrogen used in refining krypton and xenon.
Disclosure of Invention
The invention aims to provide a method and a device for reducing the use amount of liquid nitrogen in refining krypton-xenon, aiming at the defects in the prior art.
In order to achieve the purpose, the invention adopts the technical scheme that:
the method for reducing the use amount of liquid nitrogen in krypton-xenon refining is provided, wherein a cold source of a condensation evaporator in a fractionating tower is low-temperature gas obtained by mixing liquid nitrogen and nitrogen, and the low-temperature nitrogen and normal-temperature nitrogen in the cold source of the condensation evaporator of each rectifying tower are mixed in different proportions according to different operating temperatures of each rectifying tower in the fractionating tower.
Preferably, the nitrogen from each condensing evaporator is collected and then reheated by the main heat exchanger for direct emptying.
Preferably, the nitrogen from each condensing evaporator is collected and then reheated by the main heat exchanger and sent to the circulating compressor for pressurization.
Preferably, the nitrogen gas enters the main heat exchanger in the cold box after coming out of the direct pipeline gas supply or the circulating compressor.
Preferably, the nitrogen is pumped out from the cold end of the main heat exchanger and then enters a first condensing evaporator of the primary rectifying tower to be mixed with liquid nitrogen to generate low-temperature nitrogen.
Preferably, the nitrogen is pumped out from the middle part of the main heat exchanger and then enters the cold box to generate the nitrogen with lower temperature.
Preferably, the low-temperature nitrogen is a cold source of a first condensation evaporator in the primary rectifying tower.
Preferably, the low-temperature nitrogen gas is mixed with the lower-temperature nitrogen gas after exiting the first condensation evaporator to form a cold source of the condensation evaporator in the other rectifying tower.
Also provides a device for reducing the use amount of liquid nitrogen in refining krypton-xenon, which comprises:
a fractionation column for krypton-xenon purification comprising:
the first condensation evaporator is positioned in the first-stage rectifying tower and takes low-temperature gas obtained after mixing liquid nitrogen and nitrogen as a cold source; and
the second condensation evaporator, the third condensation evaporator, the fourth condensation evaporator and the fifth condensation evaporator are respectively positioned in the secondary rectification tower, the pure krypton tower, the crude xenon tower and the pure xenon tower, and the lower-temperature gas obtained by mixing low-temperature nitrogen and normal-temperature nitrogen in different proportions is used as a cold source;
the main heat exchanger is used for collecting the nitrogen from each condensation evaporator and reheating the nitrogen;
wherein the primary rectifying tower is connected with the secondary rectifying tower;
the second-stage rectifying tower is respectively connected with the pure krypton tower and the crude xenon tower;
the crude xenon tower is connected with the pure xenon tower;
the fractionating tower is connected with the main heat exchanger.
Preferably, the method further comprises the following steps:
the circulating compressor is used for receiving the reheated nitrogen and boosting the pressure;
wherein the recycle compressor is connected to the fractionation column and the main heat exchanger, respectively.
By adopting the technical scheme, compared with the prior art, the invention has the following technical effects:
the device for reducing the usage amount of liquid nitrogen in the refining of krypton-xenon comprises a circulating compressor, a fractionating tower, a main heat exchanger, a primary rectifying tower, a secondary rectifying tower, a pure krypton tower, a crude xenon tower, a pure xenon tower, a first condensation evaporator, a second condensation evaporator, a third condensation evaporator, a fourth condensation evaporator and a fifth condensation evaporator. The middle part of the main heat exchanger can pump out high-temperature nitrogen as temperature-adjusting heat flow, so that the cold quantity of liquid nitrogen is recovered, and the consumption of the liquid nitrogen refined by krypton and xenon is greatly reduced.
Drawings
FIG. 1 is a schematic diagram of an apparatus for reducing the amount of liquid nitrogen used in the purification of krypton-xenon according to the present invention;
wherein the reference numerals are:
a circulation compressor 1; a fractionating tower 2; a main heat exchanger 3; a primary rectifying tower 4; a secondary rectifying tower 5; a pure krypton column 6; a crude xenon column 7; a pure xenon column 8; a first condenser-evaporator 9; a second condenser-evaporator 10; a third condensing evaporator 11; a fourth condenser-evaporator 12; a fifth condenser-evaporator 13.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
It should be noted that the embodiments and features of the embodiments may be combined with each other without conflict.
The invention is further described with reference to the following drawings and specific examples, which are not intended to be limiting.
Example 1
As shown in fig. 1, an embodiment of the present invention provides a method for reducing the usage amount of liquid nitrogen in krypton-xenon refining, a cold source of a condensation evaporator in a fractionating tower is a low-temperature gas obtained by mixing liquid nitrogen and nitrogen, and the low-temperature nitrogen and normal-temperature nitrogen in the cold source of the condensation evaporator in each fractionating tower are mixed in different proportions according to different operating temperatures of each fractionating tower 2.
As a preferred embodiment, nitrogen gas from each condensation evaporator is collected and then reheated to 0-20 ℃ by a main heat exchanger 3, and then sent to a circulating compressor 1 to be pressurized to 0.4-0.8 MPa.
As a preferred embodiment, the nitrogen gas exits the direct pipe feed or recycle compressor 1 and enters the main heat exchanger 3 in the cold box.
As a preferred embodiment, the nitrogen is extracted from the cold end of the main heat exchanger 3 and enters the first condensing evaporator 9 of the first-stage rectifying tower 4 to be mixed with liquid nitrogen to generate low-temperature nitrogen, and the temperature is about-117.7 ℃.
As a preferred embodiment, the nitrogen is pumped out from the middle part of the main heat exchanger 3 and enters the cold box to generate lower-temperature nitrogen at the temperature of-70 ℃.
As a preferred embodiment, the low-temperature nitrogen is a cold source of a first condensation evaporator 9 in a first-stage rectifying tower 4, wherein the mixture ratio is 420 N.m3H nitrogen at-118 ℃ and 200 Nm3The low-temperature nitrogen gas with the temperature of minus 180 ℃ of 320 N.m is obtained by using liquid nitrogen/h3/h。
According to the embodiment, the mixed gas of the liquid nitrogen and the nitrogen is used as a cold source, so that the operation temperature of each condensation evaporator can be stably maintained, and the rectification is ensured to be smoothly carried out; by pre-cooling the nitrogen with higher temperature, the cold energy of the nitrogen out of the main heat exchanger 3 is recovered, the temperature is-35 ℃, the temperature is increased to-12 ℃ or even higher, the using amount of the liquid nitrogen is 250L/h, the using amount of the liquid nitrogen is reduced to 150L/h (or lower), and the reduction amplitude is 40%. And great economic benefits are generated.
By recycling the nitrogen, the consumption of liquid nitrogen or nitrogen in the krypton-xenon refining process can be greatly reduced, so that the energy consumption and the production cost are reduced. The amount of circulating nitrogen at least accounts for over 70 percent of the use amount of the system, and the saving amount of liquid nitrogen is at least 70 percent.
Example 2
As shown in fig. 1, an embodiment of the present invention further provides an apparatus for reducing liquid nitrogen usage in refining krypton and xenon, including:
a fractionation column 2 for krypton-xenon purification comprising:
a first condensation evaporator 9 which is positioned in the first-stage rectifying tower 4 and takes low-temperature gas obtained after mixing liquid nitrogen and nitrogen as a cold source; and
a second condensation evaporator 10, a third condensation evaporator 11, a fourth condensation evaporator 12 and a fifth condensation evaporator 13 which are respectively positioned in the secondary rectifying tower 5, the pure krypton tower 6, the crude xenon tower 7 and the pure xenon tower 8 and take low-temperature gas obtained by mixing low-temperature nitrogen and normal-temperature nitrogen in different proportions as cold sources;
a main heat exchanger 3 for collecting the nitrogen from each condensing evaporator and reheating the nitrogen; and
a circulating compressor 1 for receiving the reheated nitrogen gas and pressurizing;
wherein the primary rectifying tower 4 is connected with the secondary rectifying tower 5;
the secondary rectification tower 5 is respectively connected with the pure krypton tower 6 and the crude xenon tower 7;
the crude xenon tower 7 is connected with the pure xenon tower 8;
the fractionating tower 2 is connected with the main heat exchanger 3.
The recycle compressor 1 is connected to the fractionating tower 2 and the main heat exchanger 3, respectively.
After being concentrated by a front-end krypton and xenon crude device (Kr is 92.2 percent, Xe is 7.2 percent, and the balance is oxygen, nitrogen, hydrocarbon, fluoride and the like), the krypton and xenon mixture is added into a primary rectifying tower 4 in a fractionating tower 2 through a pipeline or a container (the operating pressure is 0.3MPa to 0.6MPaG, the temperature, pressure and component change influence is generally-125 to-170 ℃), low-boiling components (generally mixed oxygen, nitrogen and the like) are removed, the low-boiling components are sent into a secondary rectifying tower 5, the operating pressure of the secondary rectifying tower 5 is slightly lower than that of the primary rectifying tower 4 and is generally 0.25 to 0.5MPaG, the impurity content is reduced, the operating temperature is stable and is generally-130 ℃. The crude krypton gas is separated into high-boiling crude xenon and low-boiling crude krypton, wherein the crude krypton is sent to a pure krypton tower 6 (the operation pressure is 0.22-0.5 MPaG, the operation temperature is-135 ℃), and high-boiling components (mainly fluorides) are separated in the pure krypton tower 6 and are discharged from the bottom of the tower. Pure krypton gas (purity of over 99.999 percent in national standard) is discharged from the top of the tower and sent to the next working procedure (filling or pipeline transportation).
The crude xenon gas coming out from the bottom of the secondary rectifying tower 5 firstly enters a crude xenon tower 7 (the operation pressure is 0.03-0.2 MPaG, the operation temperature is about-100 ℃) to remove high boiling point components (hydrocarbon, partial fluoride and the like), and pure xenon gas is obtained from the top of the crude xenon tower 7 (the operation pressure is 0.02-0.2 MPaG, the operation temperature is about-100 ℃) and enters a pure xenon tower 8 (the operation pressure is 0.02-0.2 MPaG, the operation temperature is about-100 ℃). The low-boiling components are removed again in the pure xenon column 8, and pure xenon (purity of over 99.999 percent in national standard) is extracted from the bottom of the column and sent to the next working procedure (filling or pipeline transportation).
Wherein, the first-stage rectifying tower 4 and the second-stage rectifying tower 5 work, and gas rising at the bottom of the tower and liquid falling at the top of the tower are necessary conditions for the normal work of the rectifying tower. The flow of krypton and xenon refining equipment is generally small, and ascending gas is generally obtained by heating liquid by an electric heater at the bottom of a tower; the descending liquid is obtained by condensing the gas at the top of each rectifying tower through a respective condensing evaporator.
While the invention has been described with reference to a preferred embodiment, it will be understood by those skilled in the art that various changes in form and detail may be made therein without departing from the spirit and scope of the invention.
Claims (10)
1. A method for reducing the usage amount of liquid nitrogen in refining krypton-xenon is characterized in that a cold source of a condensation evaporator in a fractionating tower is low-temperature gas obtained by mixing liquid nitrogen and nitrogen, and the low-temperature nitrogen and normal-temperature nitrogen in the cold source of the condensation evaporator of each rectifying tower are mixed in different proportions according to different operating temperatures of each rectifying tower in the fractionating tower.
2. The method for reducing the usage amount of liquid nitrogen in krypton-xenon refining according to claim 1, wherein nitrogen gas from each condensing evaporator is collected and reheated by a main heat exchanger and directly discharged.
3. The method for reducing the usage amount of liquid nitrogen in krypton-xenon refining, as claimed in claim 1, wherein the nitrogen gas from each condensing evaporator is collected and reheated by a main heat exchanger and sent to a circulating compressor for pressurization.
4. The method for reducing the usage amount of liquid nitrogen in the refining of krypton-xenon according to claim 2 or 3, characterized in that the nitrogen enters a main heat exchanger in a cold box after coming out from a direct pipeline gas supply or a circulating compressor.
5. The method for reducing the usage amount of liquid nitrogen in krypton-xenon refining of claim 4, wherein the nitrogen is extracted from a cold end of a main heat exchanger and enters a first condensing evaporator of a primary rectifying tower to be mixed with the liquid nitrogen to generate low-temperature nitrogen.
6. The method for reducing the usage amount of liquid nitrogen in krypton-xenon refining according to claim 4, wherein the nitrogen is pumped out from the middle of the main heat exchanger and enters a cold box to generate lower-temperature nitrogen.
7. The method for reducing the use amount of liquid nitrogen in refining krypton-xenon according to claim 5, wherein the low-temperature nitrogen is a cold source of a first condensing evaporator in a primary rectifying tower.
8. The method for reducing the usage amount of liquid nitrogen in refining krypton-xenon according to claim 5 or 6, wherein the low-temperature nitrogen gas is discharged from the first condensing evaporator and then mixed with the lower-temperature nitrogen gas to be used as a cold source of the condensing evaporator in other rectifying towers.
9. A device for reducing the use amount of liquid nitrogen in refining krypton-xenon is characterized by comprising the following components:
a fractionation column for krypton-xenon purification comprising:
the first condensation evaporator is positioned in the first-stage rectifying tower and takes low-temperature gas obtained after mixing liquid nitrogen and nitrogen as a cold source; and
the second condensation evaporator, the third condensation evaporator, the fourth condensation evaporator and the fifth condensation evaporator are respectively positioned in the secondary rectification tower, the pure krypton tower, the crude xenon tower and the pure xenon tower, and the lower-temperature gas obtained by mixing low-temperature nitrogen and normal-temperature nitrogen in different proportions is used as a cold source;
the main heat exchanger is used for collecting the nitrogen from each condensation evaporator and reheating the nitrogen;
wherein the primary rectifying tower is connected with the secondary rectifying tower;
the second-stage rectifying tower is respectively connected with the pure krypton tower and the crude xenon tower;
the crude xenon tower is connected with the pure xenon tower;
the fractionating tower is connected with the main heat exchanger.
10. The apparatus of claim 9, further comprising:
the circulating compressor is used for receiving the reheated nitrogen and boosting the pressure;
wherein the recycle compressor is connected to the fractionation column and the main heat exchanger, respectively.
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| CN201911143252.9A CN111023697A (en) | 2019-11-20 | 2019-11-20 | Method and device for reducing liquid nitrogen usage amount in refining of krypton and xenon |
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| CN201911143252.9A CN111023697A (en) | 2019-11-20 | 2019-11-20 | Method and device for reducing liquid nitrogen usage amount in refining of krypton and xenon |
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN202757382U (en) * | 2012-07-04 | 2013-02-27 | 开封空分集团有限公司 | Carbon monoxide combination gas purifying device |
| US20180023890A1 (en) * | 2015-02-19 | 2018-01-25 | Linde Aktiengesellschaft | Method And Apparatus For Obtaining A Compressed Nitrogen Product |
| CN108106326A (en) * | 2018-01-18 | 2018-06-01 | 瀚沫能源科技（上海）有限公司 | The method and its device of nitrogen are recycled in a kind of krypton xenon process for refining |
| CN208771120U (en) * | 2018-02-12 | 2019-04-23 | 上海联风能源科技有限公司 | The device of radon is removed in a kind of krypton xenon extraction process |
| CN209428132U (en) * | 2018-11-09 | 2019-09-24 | 瀚沫能源科技（上海）有限公司 | The equipment of concentrated krypton-xenon concentrate in a kind of liquid oxygen |
-
2019
- 2019-11-20 CN CN201911143252.9A patent/CN111023697A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN202757382U (en) * | 2012-07-04 | 2013-02-27 | 开封空分集团有限公司 | Carbon monoxide combination gas purifying device |
| US20180023890A1 (en) * | 2015-02-19 | 2018-01-25 | Linde Aktiengesellschaft | Method And Apparatus For Obtaining A Compressed Nitrogen Product |
| CN108106326A (en) * | 2018-01-18 | 2018-06-01 | 瀚沫能源科技（上海）有限公司 | The method and its device of nitrogen are recycled in a kind of krypton xenon process for refining |
| CN208771120U (en) * | 2018-02-12 | 2019-04-23 | 上海联风能源科技有限公司 | The device of radon is removed in a kind of krypton xenon extraction process |
| CN209428132U (en) * | 2018-11-09 | 2019-09-24 | 瀚沫能源科技（上海）有限公司 | The equipment of concentrated krypton-xenon concentrate in a kind of liquid oxygen |
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