CN216769947U - A deoxidization system for crude argon gas - Google Patents

A deoxidization system for crude argon gas Download PDF

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Publication number
CN216769947U
CN216769947U CN202221185594.4U CN202221185594U CN216769947U CN 216769947 U CN216769947 U CN 216769947U CN 202221185594 U CN202221185594 U CN 202221185594U CN 216769947 U CN216769947 U CN 216769947U
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outlet
gas
precooler
inlet
deoxygenation tower
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闫红伟
张亚清
崔增涛
银延蛟
吕书山
郑梦杰
马明明
何新宾
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Henan Xinlianxin Shenleng Energy Co ltd
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Henan Xinlianxin Shenleng Energy Co ltd
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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
    • F25J3/04369—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 argon or argon enriched stream
    • 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
    • F25J3/04733—Producing pure argon, e.g. recovered from a crude argon column using a hybrid system, e.g. using adsorption, permeation or catalytic reaction
    • 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
    • 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/62—Details of storing a fluid in a tank

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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)
  • Chemical Kinetics & Catalysis (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

The utility model belongs to a crude argon deoxidizing system; the device comprises a raw material gas pipeline, wherein the raw material gas pipeline is connected with a Roots blower through a raw material gas buffer tank, and the Roots blower is connected with a hydrodeoxygenation unit for reducing the oxygen content in the raw material gas through a deoxygenation tower unit for removing most of oxygen in sequence; the deoxygenation tower unit comprises a deoxygenation tower part and a reboiler part matched with the deoxygenation tower part; the device has the characteristics of simple structure, reasonable flow design, reduction of the occupied area of equipment, reduction of production cost, convenience in operation and control, capability of effectively solving the problems depending on the original air separation equipment in the prior art, capability of effectively removing oxygen impurities on the premise of reducing cost and improving safety, and capability of avoiding the defect that the external liquid nitrogen is needed because the original air separation equipment is not used.

Description

A deoxidization system for crude argon gas
Technical Field
The utility model belongs to the technical field of crude argon purification, and particularly relates to a crude argon deoxidizing system.
Background
Argon is a colorless and tasteless inert gas, does not react with other substances at normal temperature, is not dissolved in liquid metal at high temperature, and can show the superiority when welding nonferrous metals; the most common welding modes of hoisting equipment are mixed gas shielded welding and submerged arc automatic welding, wherein argon is used as a shielding gas in the welding process, so that burning loss of alloy elements and other welding defects caused by the burning loss can be avoided, and metallurgical reaction in the welding process is simple and easy to control, so as to ensure high quality of welding.
At present, the most widely used argon extraction method is full-rectification argon preparation, and the basic principle is to separate oxygen and argon in a crude argon column and nitrogen and argon in a pure argon column by utilizing the difference of boiling points of oxygen-argon and nitrogen-argon. In the past, the application of argon products is not widely developed within a long period of time, the demand of the argon products is less, and the addition of an argon extraction system not only increases the investment cost of users, but also has more complex actual operation than air separation which only produces oxygen and nitrogen, has higher requirement on the operation level of operators and high operation cost, so most users do not consider adopting the argon extraction air separation. In recent years, pure argon is widely applied in many places, the demand of argon products is increased, the market prospect is good, users who do not perform argon air separation originally increase argon extraction systems in many places, and the argon extraction systems are increased in the original air.
The existing methods for deoxygenating crude argon feed gas mainly comprise two forms: 1. the aim of removing oxygen is achieved by the reaction of oxygen and hydrogen in a mode of hydrogenation in the crude argon feed gas; the method has the characteristics of cold energy saving, low energy consumption and strong oxygen removal capacity; however, the above method has a great risk in actual operation, that is, there is a risk of explosion in the reaction of hydrogen and oxygen, and there are high requirements for relevant equipment and operation risks; on the other hand, the easy formation of hydrogen-oxygen mixture increases the difficulty of subsequent processes in removing the hydrogen-oxygen mixture; 2. the method for removing oxygen by the oxygen removal tower can be seen in the following authorization notice numbers: CN 209857515U, authorized announcement date: 2019.12.27, the patent names: a device for purifying and recovering argon by full rectification; in the device, the deoxidation treatment is directly carried out through a deoxidation tower; the above method has the advantage of safe operation, but has the following disadvantages: (1) a cold source and a heat source in the air separation system need to be used, and the air separation system needs to be matched with a corresponding air separation device in the actual operation process, so that the problems of large floor area and large operation difficulty of the whole system exist; (2) if the cold energy in the air separation system is not used, an outsourcing cold source and heat source are needed, and the production cost of enterprises is increased invisibly; (3) meanwhile, deoxidation through the deoxidation tower has the defects of high energy consumption and incomplete oxygen removal.
SUMMERY OF THE UTILITY MODEL
The utility model aims to overcome the defects in the prior art, and provides the oxygen removal system for the crude argon, which can reduce the oxygen content in the crude argon to 0.1ppm, is free from being connected with the conventional air separation device and external supplement of cold source heat sources such as liquid nitrogen and the like, reduces energy consumption, and is safe and stable in operation.
The purpose of the utility model is realized as follows:
a deoxygenation system for crude argon comprises a raw material gas pipeline, wherein the raw material gas pipeline is connected with a Roots blower through a raw material gas buffer tank, and the Roots blower is connected with a hydrodeoxygenation unit for reducing the oxygen content in the raw material gas through a deoxygenation tower unit for removing most of oxygen in sequence; the deoxygenation tower unit comprises a deoxygenation tower part and a reboiler part used for matching with the deoxygenation tower part; the deoxygenation tower part comprises a deoxygenation tower, the inlet of the deoxygenation tower is connected with the outlet of the Roots blower through the first outlet of the precooler and the first inlet of the precooler, the gas phase outlet at the top of the deoxygenation tower is connected with a supercharger through the second inlet of the precooler and the second outlet of the precooler, and the outlet of the supercharger is respectively connected with the hydrodeoxygenation unit and the reboiler part;
and a liquid phase outlet at the bottom of the deoxygenation tower is connected with a drain pipeline sequentially through a second condenser inlet and a second condenser outlet of the condenser, a fourth precooler inlet and a fourth precooler outlet of the precooler.
Preferably, the hydrodeoxygenation unit comprises a compressor, a hydrodeoxygenation reactor, a cooling separator and a drying tower which are sequentially connected with a supercharger outlet of the deoxygenation tower part; the inlet of the hydrodeoxygenation reactor is provided with a hydrogen pipeline.
Preferably, a trace oxygen analyzer is arranged on a pipeline between the outlet of the supercharger and the compressor, and a residual hydrogen analyzer is arranged between the hydrodeoxygenation reactor and the cooling separator.
Preferably, the reboiler part comprises a reboiler, the inlet of the reboiler is connected with the outlet of the supercharger through the third outlet of the precooler and the third inlet of the precooler, the outlet of the reboiler is connected with the first gas-liquid separator, the liquid phase outlet of the first gas-liquid separator is connected with the first inlet of the condenser and the first outlet of the condenser through the liquid oxygen pump, the first outlet of the condenser is connected with the inlet of the second gas-liquid separator, and the liquid phase outlet of the second gas-liquid separator is connected with the reflux port at the upper part of the deoxygenating tower.
Preferably, the gas-phase outlet of the first gas-liquid separator is connected with the third end of a second tee joint arranged between the gas-phase outlet at the top of the deoxygenation tower and the second inlet of the precooler.
Preferably, the gas-phase outlet of the second gas-liquid separator is connected with the third end of the first tee joint arranged between the gas-phase outlet at the top of the deoxygenation tower and the second inlet of the precooler.
Preferably, a throttle valve is arranged between the liquid phase outlet at the bottom of the deoxygenation tower and the second inlet of the condenser.
The deoxygenation system for crude argon gas prepared according to the scheme realizes deoxygenation of the deoxygenation tower by taking mixed gas passing through the deoxygenation tower as a refrigeration working medium on the basis of the deoxygenation tower unit, does not need to supplement liquid nitrogen externally, enables a device to be completely independent from an air separation system, avoids purchasing liquid nitrogen externally, can overcome the defect of deoxygenation through the deoxygenation tower in the traditional technology, simultaneously adopts the coupling technology of the deoxygenation tower unit and the hydrodeoxygenation unit to remove oxygen impurities in raw material gas, effectively solves the problems of difficult separation of oxygen and argon and high energy consumption, namely the utility model adopts the purification of the deoxygenation tower to realize the purpose of removing most of the oxygen impurities, adopts a hydrodeoxygenation part on the basis to effectively remove a small amount of oxygen impurities, and has the characteristics of low reaction temperature, good safety performance, solving the hydrogen-related safety risk problem, reducing the rectification deoxygenation load and greatly reducing the investment, and can remove oxygen in the raw material gas to be below 0.1 ppm; furthermore, the utility model overcomes the problem that hydrodeoxygenation requires equipment with higher safety level in the traditional technology, and simultaneously utilizes a trace oxygen analyzer and a residual hydrogen analyzer to accurately catalyze the hydrogen-oxygen ratio of the oxidation device, thereby adjusting the control method of the hydrogenation amount and ensuring that the reaction is mild, safe and reliable; meanwhile, the explosion danger caused by overhigh oxygen content and the formation of hydrogen-oxygen mixture caused by overhigh hydrogen content are avoided; the device has the characteristics of simple structure, reasonable flow design, reduced equipment floor area, reduced production cost, convenient operation and control, capability of effectively solving the problem of relying on the original air separation equipment in the prior art, effective removal of oxygen impurities on the premise of reducing cost and improving safety, and capability of avoiding the defect of external liquid nitrogen caused by the fact that the original air separation equipment is not used.
Drawings
FIG. 1 is a schematic structural diagram of the present invention.
Detailed Description
In order to more clearly understand the technical features, objects, and effects of the present invention, embodiments of the present invention will now be described with reference to the accompanying drawings, in which like reference numerals refer to like parts throughout. For the sake of simplicity, only the parts related to the utility model are schematically shown in the drawings, and they do not represent the actual structure as a product.
As shown in fig. 1, the utility model is a crude argon deoxidizing system, which comprises a raw material gas pipeline 1, wherein the raw material gas pipeline 1 is connected with a roots blower 3 through a raw material gas buffer tank 2, and the roots blower 3 is connected with a hydrodeoxygenation unit for reducing the oxygen content in the raw material gas through a deoxygenation tower unit for removing most of oxygen in turn; the deoxygenation tower unit comprises a deoxygenation tower part and a reboiler part used for matching with the deoxygenation tower part. In the utility model, crude argon in a feed gas pipeline 1 enters a raw material gas buffer tank 2 for buffering, then is pressurized by a Roots blower 3 and enters a deoxygenation tower unit for removing most of oxygen, and mixed gas passing through a deoxygenation tower part in the deoxygenation tower unit respectively enters a hydrodeoxygenation unit and a reboiler part matched with the deoxygenation tower part, namely: one part of mixed gas passing through the deoxidizing tower part is used as raw material gas to enter the reboiler part as a reboiling heat source of the reboiler part, and the other part of mixed gas is used as raw material to be further deoxidized.
Further, the deoxygenation tower part comprises a deoxygenation tower 5, an inlet of the deoxygenation tower 5 is connected with an outlet of the Roots blower 3 through a precooler first outlet 22 and a precooler first inlet 21 of the precooler 4, a gas phase outlet at the top of the deoxygenation tower 5 is connected with a supercharger 6 through a precooler second inlet 23 and a precooler second outlet 24 of the precooler 4, and outlets of the supercharger 6 are respectively connected with a hydrodeoxygenation unit and a reboiler part; and a liquid phase outlet at the bottom of the deoxygenation tower 5 is connected with the emptying pipeline 11 sequentially through a second condenser inlet 31 and a second condenser outlet 32 of the condenser 9, a fourth precooler inlet 27 and a fourth precooler outlet 28 of the precooler 4. The raw material gas is subjected to heat exchange and temperature reduction through a precooler 4 and then enters a deoxygenation tower 5 to remove most of oxygen, the gas phase after deoxygenation is subjected to reheating and pressurization, and a part of the gas phase enters a reboiler part to serve as a reboiling heat source so as to realize the normal operation of the deoxygenation tower 5; the other part of the gas phase enters a hydrodeoxygenation unit to remove the residual oxygen; the above-described method enables the gas phase in the deoxygenation column 5 to be recycled, and the gas phase can be used not only as a raw material but also as a reboiling heat source; has the characteristics of energy conservation, consumption reduction and cost reduction; most of the oxygen components in the crude argon feed gas are liquefied and collected at the bottom of the deoxygenation tower 5, and after being collected, the cold energy is recovered by a condenser 9 and a precooler 4 and is discharged outside by a discharge pipeline 11.
Further, the hydrodeoxygenation unit comprises a compressor 12, a hydrodeoxygenation reactor 13, a cooling separator 14 and a drying tower 15 which are sequentially connected with the outlet of the supercharger 6 at the deoxygenation tower part; the inlet of the hydrodeoxygenation reactor 13 is provided with a hydrogen pipeline 16. The hydrodeoxygenation unit in the utility model is a continuation of the deoxygenation tower part, can reduce the oxygen content in the raw material gas to the maximum extent, reduce the oxygen content in the raw material gas to be below 0.1ppm, and can ensure the operation safety and stability of the hydrodeoxygenation part after a large amount of oxygen is removed from the deoxygenation tower part; meanwhile, the cooling separator 14 and the drying tower 15 are arranged, so that the feed gas passing through the hydrodeoxygenation reactor 13 can be cooled and separated in time, and finally enters the drying tower 15 for drying, so that the moisture in the feed gas is controlled to be below 10ppm, and a foundation is laid for the subsequent processes.
Furthermore, a trace oxygen analyzer 17 is arranged on a pipeline between the outlet of the supercharger 6 and the compressor 12, and a residual hydrogen analyzer 18 is arranged between the hydrodeoxygenation reactor 13 and the cooling separator 14. The utility model is also provided with a trace oxygen analyzer 17 and a residual hydrogen analyzer 18, which can provide data support for the oxygen content and the hydrogen content in the gas, wherein the data support for providing the oxygen content can ensure the continuous safe and stable operation of the hydrodeoxygenation reactor 13, thereby reducing the explosion risk, and the hydrogen content can prevent the generation of oxyhydrogen mixture to influence the operation of the subsequent steps.
Further, the reboiler part comprises a reboiler 34, an inlet of the reboiler 34 is connected with an outlet of the booster 6 through a third outlet 26 of the precooler 4 and a third inlet 25 of the precooler, an outlet of the reboiler 34 is connected with the first gas-liquid separator 7, a liquid phase outlet of the first gas-liquid separator 7 is connected with a first inlet 29 of the condenser 9 and a first outlet 30 of the condenser through a liquid oxygen pump 8, the first outlet 30 of the condenser is connected with an inlet of the second gas-liquid separator 10, and a liquid phase outlet of the second gas-liquid separator 10 is connected with a reflux port 33 at the upper part of the deoxygenation tower 5. The reboiling heat source passing through the reboiler 34 is completely liquefied, and the liquefied gas is introduced into the first gas-liquid separator 7 to be subjected to gas-liquid separation, and the liquid phase after the gas-liquid separation is introduced into the second gas-liquid separator 10 to be subjected to gas-liquid separation again after passing through the condenser 9, wherein the liquid phase is introduced into the deoxygenation tower 5 as reflux liquid to be used as reflux liquid.
Further, the gas phase outlet of the first gas-liquid separator 7 is connected with the third end of a second tee 20 arranged between the gas phase outlet at the top of the deoxygenation tower 5 and the second inlet 23 of the precooler.
Further, the gas phase outlet of the second gas-liquid separator 10 is connected with the third end of the first tee 19 arranged between the gas phase outlet at the top of the deoxygenation tower 5 and the second inlet 23 of the precooler.
Further, a throttle valve 35 is arranged between the liquid phase outlet at the bottom of the deoxygenation tower 5 and the second condenser inlet 31 of the condenser 9.
The working principle of the utility model is as follows: a method for deoxygenating a crude argon deoxygenation system, the method comprising the steps of:
step 1: crude argon feed gas in the feed gas pipeline 1 enters a Roots blower 3, a precooler first inlet 21 and a precooler first outlet 22 of a precooler 4 through a feed gas buffer tank 2 and enters a deoxygenation tower 5; the content of argon in the crude argon feed gas is more than or equal to 80 percent, the content of oxygen is less than or equal to 15 percent, and the content of nitrogen is less than or equal to 5 percent; the pressure of the crude argon raw material gas pressurized by the Roots blower 3 is as follows: 1.5 to 1.8barA, wherein the temperature of the crude argon feed gas after heat exchange by the precooler 4 is-165 ℃ to-169 ℃;
step 2: the crude argon feed gas entering the deoxygenation tower 5 and reflux liquid from a reflux port 33 at the upper part of the deoxygenation tower 5 are subjected to quality change heat exchange, most of oxygen components in the crude argon feed gas are liquefied, and are continuously enriched at the bottom of the deoxygenation tower 5; the liquid level of the deoxygenation tower 5 is controlled by a throttle valve 35, and redundant liquid phase enters an emptying pipeline 11 for realizing outward discharge after cold energy recovery through a second condenser inlet 31 and a second condenser outlet 32 of the condenser 9, a fourth precooler inlet 27 and a fourth precooler outlet 28 of the precooler 4;
and step 3: the gas phase in the deoxygenation tower 5 enters a supercharger 6 through a gas phase outlet at the top of the deoxygenation tower 5, a precooler second inlet 23 of the precooler 4 and a precooler second outlet 24 for pressurization; the oxygen content in the gas phase in the deoxygenation tower 5 is less than 0.1 percent; the gas phase enters a precooler 4 to provide cold energy, and enters a supercharger 6 to be pressurized to 2.7-3.1 barA after being reheated;
and 4, step 4: a part of the gas phase passing through the supercharger 6 enters the precooler 4 to be cooled and liquefied to form a gas-liquid mixed state, then enters the reboiler 34 to be used as a reboiling heat source of the deoxygenation tower 5, is completely liquefied in the reboiler 34 and then enters the first gas-liquid separator 7 to be subjected to gas-liquid separation, the separated liquid phase enters the second gas-liquid separator 10 through the liquid oxygen pump 8 and the condenser 9, and the liquid phase subjected to gas-liquid separation by the second gas-liquid separator 10 enters the deoxygenation tower 5 through the reflux port 33 to be used as reflux liquid; the liquid phase pressure after passing through the liquid oxygen pump 8 is as follows: 4 to 7 barA;
and 5: the gas phase subjected to gas-liquid separation in the step 4 by the first gas-liquid separator 7 is connected with the third end of the second tee 20; the gas phase subjected to gas-liquid separation by the second gas-liquid separator 10 is connected with the third end of the first tee 19;
step 6: the other part of the gas phase in step 3, which is passed through booster 6, is compressed in compressor 12 to a pressure of: after 10 to 11barA, the gas is sent into a hydrogenation and deoxygenation reactor 13 from an outlet of a compressor 12, the compressed gas and hydrogen from a hydrogen pipeline 16 react under the action of a catalyst, the reaction temperature is less than 200 ℃, the oxygen content in feed gas discharged from the outlet of the hydrogenation and deoxygenation reactor 13 is reduced to be less than 0.1ppm, and the hydrogen content is controlled to be less than 1%;
in the process, the content of oxygen entering the compressor 12 is monitored in real time through a trace oxygen analyzer 17, and when the concentration of oxygen at the inlet of the compressor 12 is less than 1%, a hydrogen pipeline 16 supplies hydrogen to the hydrodeoxygenation reactor 13; when the oxygen concentration at the inlet of the nitrogen compressor 12 is more than or equal to 1%, the hydrogen pipeline 16 stops supplying hydrogen to the hydrodeoxygenation reactor 13; meanwhile, the residual hydrogen analyzer 18 detects the gas reacted by the hydrodeoxygenation reactor 13, and when the hydrogen concentration is less than 1%, the hydrogen pipeline 16 continuously supplies hydrogen to the hydrodeoxygenation reactor 13; when the hydrogen concentration is 1% or more, the hydrogen line 16 stops supplying hydrogen to the hydrodeoxygenation reactor 13;
and 7: the raw material gas discharged from the hydrodeoxygenation reactor 13 enters a cooling separator 14, heat exchange cooling is carried out through a cold medium, so that moisture in the raw material gas is condensed, the condensed raw material gas with moisture removed is dried through a drying tower 15, and the moisture in the raw material gas is controlled to be below 10 ppm; the cooling medium in the cooling separator 14 is water; and (3) feeding the raw material gas passing through the drying tower 15 into a post argon-removing purification system.
The deoxidation part of the utility model adopts a form of combining the deoxidation tower part and the hydrodeoxygenation part, can realize that the oxygen content is reduced to below 0.1ppm, abandons the problem of higher oxygen content in the raw material gas caused by deoxidation by adopting the deoxidation tower in the traditional technology, and can also solve the defect of overhigh requirement level of the hydrodeoxygenation part on equipment; the raw material gas passing through the deoxidation tower part is used as a reboiling heat source in the reboiler 34 on the basis of the combination, so that the characteristics of energy conservation and consumption reduction, no need of purchasing liquid nitrogen and cost reduction can be realized, furthermore, the trace oxygen analyzer 17 and the residual hydrogen analyzer 18 are arranged in the hydrodeoxygenation part, the analyzers can provide data support for the oxygen content and the hydrogen content in the gas, wherein the data support for providing the oxygen content can ensure the continuous safe and stable operation of the hydrodeoxygenation reactor 13, so that the explosion risk is reduced, and the hydrogen content can be provided to prevent the generation of a hydrogen-oxygen mixture so as to influence the operation of subsequent steps. The above arrangement can provide a foundation for a subsequent argon purification system.
In the description of the present invention, it is to be noted that, unless otherwise explicitly specified or limited, the terms "connected," "connecting," and the like are to be construed broadly, and may, for example, be fixedly connected, integrally connected, or detachably connected; or communication between the interior of the two elements; they may be directly connected or indirectly connected through an intermediate, and those skilled in the art can understand the specific meaning of the above terms in the present invention according to specific situations. The above examples are merely illustrative of the feasible embodiments of the present invention and they are not intended to limit the scope of the present invention, and equivalent embodiments, modifications and alterations without departing from the technical spirit of the present invention are included in the scope of the present invention.

Claims (7)

1. A deoxidization system for crude argon gas, includes feed gas pipeline (1), its characterized in that: the raw material gas pipeline (1) is connected with a Roots blower (3) through a raw material gas buffer tank (2), and the Roots blower (3) is connected with a hydrodeoxygenation unit for reducing the oxygen content in the raw material gas through a deoxygenation tower unit for removing most of oxygen in sequence;
the deoxygenation tower unit comprises a deoxygenation tower part and a reboiler part used for matching with the deoxygenation tower part;
the deoxygenation tower part comprises a deoxygenation tower (5), the inlet of the deoxygenation tower (5) is connected with the outlet of the Roots blower (3) through a precooler first outlet (22) and a precooler first inlet (21) of a precooler (4), a gas phase outlet at the top of the deoxygenation tower (5) is connected with a supercharger (6) through a precooler second inlet (23) and a precooler second outlet (24) of the precooler (4), and the outlet of the supercharger (6) is respectively connected with a hydrodeoxygenation unit and a reboiler part;
and a liquid phase outlet at the bottom of the deoxygenation tower (5) is connected with the emptying pipeline (11) sequentially through a second condenser inlet (31) of the condenser (9), a second condenser outlet (32), a fourth precooler inlet (27) of the precooler (4) and a fourth precooler outlet (28).
2. The system of claim 1 for the removal of crude argon, wherein: the hydrodeoxygenation unit comprises a compressor (12), a hydrodeoxygenation reactor (13), a cooling separator (14) and a drying tower (15), which are sequentially connected with the outlet of a supercharger (6) at the deoxygenation tower part; the inlet of the hydrodeoxygenation reactor (13) is provided with a hydrogen pipeline (16).
3. The system of claim 2, wherein: a trace oxygen analyzer (17) is arranged on a pipeline between the outlet of the supercharger (6) and the compressor (12), and a residual hydrogen analyzer (18) is arranged between the hydrodeoxygenation reactor (13) and the cooling separator (14).
4. The system of claim 1 for the removal of crude argon, wherein: the reboiler part comprises a reboiler (34), the inlet of the reboiler (34) is connected with the outlet of the supercharger (6) through a third outlet (26) of the precooler and a third inlet (25) of the precooler (4), the outlet of the reboiler (34) is connected with the first gas-liquid separator (7), the liquid phase outlet of the first gas-liquid separator (7) is connected with the first inlet (29) of the condenser (9) and the first outlet (30) of the condenser through a liquid oxygen pump (8), the first outlet (30) of the condenser is connected with the inlet of the second gas-liquid separator (10), and the liquid phase outlet of the second gas-liquid separator (10) is connected with a reflux port (33) at the upper part of the deoxygenating tower (5).
5. The system of claim 4, wherein: the gas phase outlet of the first gas-liquid separator (7) is connected with the third end of a second tee joint (20) arranged between the gas phase outlet at the top of the deoxygenation tower (5) and the second inlet (23) of the precooler.
6. The system of claim 4, wherein: the gas phase outlet of the second gas-liquid separator (10) is connected with the third end of a first tee joint (19) arranged between the gas phase outlet at the top of the deoxygenation tower (5) and the second inlet (23) of the precooler.
7. The system of claim 1 for the removal of crude argon, wherein: a throttle valve (35) is arranged between the liquid phase outlet at the bottom of the deoxygenation tower (5) and the second condenser inlet (31) of the condenser (9).
CN202221185594.4U 2022-05-18 2022-05-18 A deoxidization system for crude argon gas Active CN216769947U (en)

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