CN218001968U - Condensation liquefying device for recovering diffused oxygen nitrogen argon gas - Google Patents
Condensation liquefying device for recovering diffused oxygen nitrogen argon gas Download PDFInfo
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- CN218001968U CN218001968U CN202222129754.XU CN202222129754U CN218001968U CN 218001968 U CN218001968 U CN 218001968U CN 202222129754 U CN202222129754 U CN 202222129754U CN 218001968 U CN218001968 U CN 218001968U
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Abstract
The utility model belongs to a condensing and liquefying device for recovering oxygen, nitrogen and argon gas diffused; the device comprises an air separation device, wherein the air separation device is respectively connected with a liquid oxygen storage tank, a liquid nitrogen storage tank and a liquid argon storage tank through pipelines, and a gas phase outlet of the liquid oxygen storage tank is connected with the liquid oxygen storage tank through an oxygen liquefaction channel of a condenser; a gas phase outlet of the liquid argon storage tank is connected with the liquid argon storage tank through an argon liquefying channel of the condenser; a liquid nitrogen outlet of the liquid nitrogen storage tank is connected with a shell pass of the condenser, a shell pass gas phase outlet of the condenser is connected with the liquefaction unit, and an outlet of the liquefaction unit is connected with the liquid nitrogen storage tank; the gas tank storage device has the advantages of simple structure, reasonable design, simplicity and flexibility in operation and control, reduction in production cost of enterprises on the premise of ensuring safe storage of the gas tank, stability of liquid-phase products, improvement of product utilization rate and avoidance of resource waste.
Description
Technical Field
The utility model belongs to the technical field of air separation storage, concretely relates to retrieve condensation liquefaction device who disperses oxygen nitrogen argon gas.
Background
At present, liquid phase products produced by a large air separation plant are generally conveyed to a corresponding storage tank through a pipeline for storage, and gas generated by the natural evaporation of the liquid phase products in the storage tank and the cold loss in the conveying process of the pipeline can be stored in the storage tank together with the liquid phase products; if the corresponding gas quantity is too large, the safe storage of the storage tank is threatened, and on the basis, a breather valve is installed at the top of the storage tank, namely, the gas is discharged when the pressure of the gas is too large; above-mentioned installation breather valve is only in order to guarantee the setting that the storage tank safety goes on, can't retrieve the gaseous of gasification, has not only increased the manufacturing cost of enterprise to the liquid phase, and has wasted liquid phase product resource.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to overcome the defect among the prior art, and provide one kind through utilizing the boiling point difference of oxygen, nitrogen, the argon material that air separation plant produced as the basis, make liquid nitrogen liquefied oxygen, argon gas and carry out the backward flow, carry out the liquefaction processing to gas nitrogen through the liquefaction unit simultaneously to realize reducing enterprise manufacturing cost, liquid phase product stability, improve product utilization and avoid the wasting of resources's recovery to disperse the condensing liquefying device of oxygen nitrogen argon gas.
The purpose of the utility model is realized like this:
a condensation liquefaction device for recovering diffused oxygen-nitrogen-argon gas comprises an air separation device, wherein the air separation device is respectively connected with a liquid oxygen storage tank, a liquid nitrogen storage tank and a liquid argon storage tank through pipelines, and a top gas-phase outlet of the liquid oxygen storage tank is connected with a liquid-phase return port of the liquid oxygen storage tank through an oxygen liquefaction passage of a condenser; a top gas phase outlet of the liquid argon storage tank is connected with a liquid phase reflux port of the liquid argon storage tank through an argon liquefaction channel of the condenser; a liquid nitrogen outlet at the lower part of the liquid nitrogen storage tank is connected with a shell pass of the condenser, a shell pass gas phase outlet of the condenser is connected with the liquefaction unit, and an outlet of the liquefaction unit is connected with a third end of a first tee joint arranged between the air separation device and the liquid nitrogen storage tank; the third end of the first tee is also connected with a shell side liquid phase outlet of the condenser; and a second tee joint is arranged between the shell pass of the condenser and the liquefaction unit, and the third end of the second tee joint is connected with a top gas-phase outlet of the liquid nitrogen storage tank.
Preferably, the liquefaction unit comprises a buffer tank, an outlet of the buffer tank is connected with a circulating compressor, a pressurizing end of an expander and a cooler through a third tee joint, a second end of the third tee joint is connected with a gas-liquid separator through a first channel of a plate heat exchanger and a throttle valve, and a liquid phase outlet of the gas-liquid separator is connected with a pipeline between the air separation device and the liquid nitrogen storage tank; and the second end of the second tee joint is connected with the inlet of the buffer tank.
Preferably, the third end of the third tee is connected with the inlet of the low-temperature refrigerating device through the second channel of the plate heat exchanger, the outlet of the low-temperature refrigerating device is connected with the expansion end of the expander through the third channel of the plate heat exchanger, and the outlet of the expansion end of the expander is connected with the inlet of the buffer tank through the fourth channel of the plate heat exchanger; and the second end of the second tee joint is connected with the inlet of the buffer tank through a fifth channel of the plate heat exchanger.
Preferably, the plate heat exchanger, the expansion end of the expander, the throttle valve and the gas-liquid separator are arranged in the cold box.
Preferably, an oxygen emptying pipeline with an oxygen emptying valve is arranged at the inlet of the oxygen liquefying channel; an argon gas emptying pipeline with an argon gas emptying valve is arranged at the inlet of the argon liquefying channel; and a shell pass gas phase outlet of the condenser is provided with a nitrogen emptying pipeline with a nitrogen emptying valve.
Preferably, a fourth tee joint and a liquid nitrogen booster pump are sequentially arranged between a liquid nitrogen outlet at the lower part of the liquid nitrogen storage tank and the shell pass of the condenser, and a first nitrogen pipeline connected with the liquid nitrogen storage tank is arranged on a gas outlet pipeline of the liquid nitrogen booster pump; the third end of the fourth tee joint is connected with the liquid nitrogen flushing vehicle through a liquid nitrogen charging pump, and a second nitrogen pipeline connected with a liquid nitrogen storage tank is arranged on a gas outlet pipeline of the liquid nitrogen charging pump.
Preferably, a liquid oxygen outlet at the lower part of the liquid oxygen storage tank is connected with the liquid oxygen flushing tank vehicle through a liquid oxygen charging pump; an oxygen pipeline connected with the liquid oxygen storage tank is arranged on a gas outlet pipeline of the liquid oxygen charging pump.
Preferably, a liquid argon outlet at the lower part of the liquid argon storage tank is connected with a liquid argon flushing tank vehicle through a liquid argon filling pump; and an argon pipeline connected with the liquid argon storage tank is arranged on a gas outlet pipeline of the liquid argon filling pump.
The utility model discloses a retrieve condensation liquefaction device who disperses oxygen nitrogen argon gas who makes according to above-mentioned scheme, the utility model discloses the liquid phase product storage that large-scale air separation system separates uses, and it specifically liquefies in order to solve in the conventional art directly through the form of unloading and cause cost-push and the wasting of resources to the cold loss of liquid phase product in the pipeline transportation process and the gaseous of liquid natural evaporation production; in particular, the utility model uses the boiling point difference of oxygen, nitrogen and argon as the basis to lead the liquid nitrogen to liquefy oxygen and argon gas and carry out reflux, and simultaneously, the liquefaction unit liquefies the gas nitrogen; the mode can achieve the purposes of reducing the production cost of enterprises, stabilizing liquid-phase products, improving the utilization rate of the products, avoiding resource waste and ensuring the safety of corresponding storage tanks without purchasing a cold source on the premise of not changing the original air separation equipment; furthermore, the utility model also comprises the gas phase generated in the canned liquid phase product for the liquefaction of the gas phase, so as to achieve the characteristic of improving the recovery rate of the liquid phase product; the utility model further uses the liquefaction unit to ensure that the liquid phase product in the storage tank does not contain gas phase by performing step cooling and gas-liquid separation on the basis of the cooling medium which takes nitrogen as gas and nitrogen, thereby realizing the liquefaction of the gas and the nitrogen and ensuring the purity of the liquid phase product; the utility model also considers the safety and economy of the whole condensation liquefaction device, when the gas phase of the gas oxygen and/or the gas argon passes through the condenser, the pressure of the gas oxygen and/or the gas argon can be still overhigh and solved by adopting the form of simultaneous emptying; when the liquid nitrogen is used for condensing gas oxygen and/or gas argon in a condenser, if the quantity of the generated gas nitrogen is too small, the price of the quantity of the condensed liquid nitrogen is insufficient for starting a liquefying unit, and the gas nitrogen can be subjected to emptying treatment in order to consider the economical efficiency; the gas tank storage device has the advantages of simple structure, reasonable design, simplicity and flexibility in operation, reduction in production cost of enterprises on the premise of ensuring safe storage of the gas tank, stability of liquid-phase products, improvement of product utilization rate and avoidance of resource waste.
Drawings
Fig. 1 is a schematic structural diagram of the present invention.
Fig. 2 is a schematic diagram of the liquefaction unit of the present invention.
Detailed Description
In order to clearly understand the technical features, objects, and effects of the present invention, embodiments of the present invention will be described with reference to the accompanying drawings, in which like reference numerals refer to like parts in the drawings. 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 and 2, the utility model relates to a condensation liquefaction device for recovering diffused oxygen-nitrogen-argon gas, which comprises an air separation device 1, wherein the air separation device 1 is respectively connected with a liquid oxygen storage tank 2, a liquid nitrogen storage tank 3 and a liquid argon storage tank 4 through pipelines, and a top gas phase outlet of the liquid oxygen storage tank 2 is connected with a liquid phase reflux port of the liquid oxygen storage tank 2 through an oxygen liquefaction passage 6 of a condenser 5; a gas phase outlet at the top of the liquid argon storage tank 4 is connected with a liquid phase reflux port of the liquid argon storage tank 4 through an argon liquefaction channel 7 of the condenser 5; a liquid nitrogen outlet at the lower part of the liquid nitrogen storage tank 3 is connected with a shell pass of the condenser 5, a shell pass gas phase outlet of the condenser 5 is connected with the liquefaction unit, and an outlet of the liquefaction unit is connected with a third end of a first tee joint 8 arranged between the air separation device 1 and the liquid nitrogen storage tank 3; the third end of the first tee joint 8 is also connected with a shell-side liquid phase outlet of the condenser 5; and a second tee joint 9 is arranged between the shell pass of the condenser 5 and the liquefaction unit, and the third end of the second tee joint 9 is connected with a top gas-phase outlet of the liquid nitrogen storage tank 3. The utility model provides a technical scheme to the gaseous phase in nitrogen, oxygen, argon liquid phase product storage tank is liquefied and is retrieved, this technical scheme can realize guaranteeing the operation safety of each storage tank, simultaneously the utility model discloses utilize the boiling point difference of nitrogen, oxygen, argon, liquefy gas oxygen and argon on the basis of liquid nitrogen, this mode need not to purchase the cold source outward and can realize reducing the manufacturing cost of liquid phase product on the basis of not changing original air separation system again, improve the rate of recovery of liquid phase product, avoid the wasting of resources and the stable stability of liquid phase product; specifically, oxygen and argon are subjected to heat exchange condensation through liquid nitrogen, and gas nitrogen subjected to heat exchange is condensed through a liquefaction unit; and refluxing the condensed liquid-phase product into respective storage tanks for sale.
Further, the liquefaction unit comprises a buffer tank 10, an outlet of the buffer tank 10 is connected with a circulating compressor 11, a pressurizing end 12 of an expansion machine and a cooler 13 through a third tee 14, a second end of the third tee 14 is connected with a gas-liquid separator 38 through a first channel of a plate heat exchanger 15 and a throttle valve 36, and a liquid phase outlet of the gas-liquid separator 38 is connected with a pipeline between the air separation device 1 and the liquid nitrogen storage tank 3; the second end of the second tee joint 9 is connected with the inlet of a buffer tank 10. The utility model provides a gaseous nitrogen not only can progressively realize the condensation liquefaction to gaseous nitrogen through pressure boost, heat transfer and gas-liquid separation's form, thereby this mode can avoid smuggleing the quality that nitrogen gas influences liquid phase product in liquid nitrogen storage tank 3 secretly in the liquid phase product.
Further, a third end of the third tee 14 is connected with an inlet of a low-temperature refrigeration device 16 through a second channel of the plate heat exchanger 15, an outlet of the low-temperature refrigeration device 16 is connected with an expansion end 17 of an expander through a third channel of the plate heat exchanger 15, and an outlet of the expansion end 17 of the expander is connected with an inlet of the buffer tank 10 through a fourth channel of the plate heat exchanger 15; the second end of the second tee joint 9 is connected with the inlet of the buffer tank 10 through a fifth channel of the plate heat exchanger 15. The utility model discloses at first, utilize nitrogen gas can realize avoiding outsourcing air supply can also prevent to take place to leak and influence the problem of liquid phase product quality simultaneously as coolant, secondly, the nitrogen gas as heat transfer medium passes through the expansion end 17 of low temperature refrigerating plant 16 and expander and carries out the step heat transfer with the product in twice entering plate heat exchanger 15 to realize improving gas nitrogen condensation effect and avoiding appearing gaseous problem in the liquid nitrogen.
Further, the plate heat exchanger 15, the expansion end 17 of the expander, the throttle 36, and the gas-liquid separator 38 are disposed in the cold box 37. Through the arrangement, the utilization efficiency of a cold source can be improved, and the effect of heat exchange with the outside is reduced as much as possible.
Further, an oxygen emptying pipeline 19 with an oxygen emptying valve 18 is arranged at the inlet of the oxygen liquefying channel 6; an argon gas emptying pipeline 21 with an argon gas emptying valve 20 is arranged at the inlet of the argon liquefying channel 7; and a nitrogen vent pipeline 23 with a nitrogen vent valve 22 is arranged at the shell-side gas-phase outlet of the condenser 5. The purpose of flexible operation can be realized on the premise of considering the safety and the economical efficiency of the whole system through the arrangement.
Furthermore, a fourth tee joint 24 and a liquid nitrogen booster pump 25 are sequentially arranged between a liquid nitrogen outlet at the lower part of the liquid nitrogen storage tank 3 and the shell pass of the condenser 5, and a first nitrogen pipeline 26 connected with the liquid nitrogen storage tank 3 is arranged on a gas outlet pipeline of the liquid nitrogen booster pump 25; the third end of the fourth tee 24 is connected with a liquid nitrogen flushing tank truck 28 through a liquid nitrogen filling pump 27, and a second nitrogen pipeline 29 connected with the liquid nitrogen storage tank 3 is arranged on a gas outlet pipeline of the liquid nitrogen filling pump 27.
Further, a liquid oxygen outlet at the lower part of the liquid oxygen storage tank 2 is connected with a liquid oxygen flushing tank car 31 through a liquid oxygen charging pump 30; an oxygen pipeline 32 connected with the liquid oxygen storage tank 2 is arranged on the gas outlet pipeline of the liquid oxygen charging pump 30.
Further, a liquid argon outlet at the lower part of the liquid argon storage tank 4 is connected with a liquid argon flushing tank car 34 through a liquid argon filling pump 33; and an argon gas pipeline 35 connected with the liquid argon storage tank 4 is arranged on a gas outlet pipeline of the liquid argon filling pump 33.
The condensation liquefaction method of the condensation liquefaction device comprises the following steps:
step 1: oxygen, nitrogen and argon liquid products produced by the air separation device 1 respectively enter a liquid oxygen storage tank 2, a liquid nitrogen storage tank 3 and a liquid argon storage tank 4 through pipeline conveying, and gas enters the tops of the corresponding storage tanks to be gathered in the process of pipeline conveying of the oxygen, nitrogen and argon liquid products and is naturally volatilized after the products enter the corresponding storage tanks, so that the top pressure of the corresponding storage tanks is increased;
step 2: the gas phase in the liquid oxygen storage tank 2 exchanges heat with liquid nitrogen in the shell pass of the condenser 5 through an oxygen liquefaction channel 6 of the condenser 5, and the liquid oxygen discharged from the outlet of the oxygen liquefaction channel 6 after heat exchange enters the liquid oxygen storage tank 2 through a liquid phase reflux port of the liquid oxygen storage tank 2; the gas phase at the top gas phase outlet of the liquid oxygen storage tank 2 is gas oxygen, and the temperature is as follows: -178 ℃, pressure: 10-26 kpa, and the flow rate of oxygen is 125NM 3 /h～135NM 3 H; liquid nitrogen is filled in the shell pass of the condenser 5, the temperature is-186 ℃, and the pressure is 170kpa; the liquid oxygen temperature through the liquid phase return port of the liquid oxygen storage tank 2 is: -183 ℃, pressure: 23KPA;
and 3, step 3: the gas phase in the liquid argon storage tank 4 exchanges heat with liquid nitrogen in the shell pass of the condenser 5 through an argon liquefying channel 7 of the condenser 5, and liquid argon discharged from the outlet of the argon liquefying channel 7 after heat exchange enters the liquid argon storage tank 4 through a liquid phase reflux port of the liquid argon storage tank 4; the gas phase at the top gas phase outlet of the liquid argon storage tank 4 is gas argon, and the temperature is as follows: -181 ℃, pressure: 10-26 kpa, flow rate: 125NM 3 /h～135NM 3 H; liquid nitrogen is filled in the shell pass of the condenser 5, the temperature is-186 ℃, and the pressure is 170kpa; the liquid argon temperature through the liquid phase return port of the liquid argon storage tank 4 is as follows: -183 ℃, pressure: 23KPA;
and 4, step 4: the liquid nitrogen in the shell pass of the condenser 5 in the step 2 and/or the step 3 comes from the liquid nitrogen storage tank 3, a liquid nitrogen outlet at the lower part of the liquid nitrogen storage tank 3 enters the shell pass of the condenser 5 through a fourth tee joint 24 and a liquid nitrogen booster pump 25 for heat exchange, and the liquid nitrogen is converted into gas nitrogen after the heat exchange in the step 2 and/or the step 3, and the temperature of the gas nitrogen is as follows: -186 ℃, pressure: 170kpa, flow rate 1500Nm 3 /h；
And 5: after the gas nitrogen in the step 4 and the gas nitrogen lost in the pipeline conveying process in the step 1 and naturally volatilized by the liquid nitrogen storage tank 3 are converged at the second tee joint 9, heat exchange is carried out through a fifth channel of the plate heat exchanger 15, and the gas nitrogen after heat exchange and the circulating nitrogen gas jointly enter the buffer tank 10;
step 6: after the gas nitrogen in the buffer tank 10 is pressurized to 1.2Mpa by the circulating compressor 11, the gas nitrogen enters the pressurization end 12 of the expansion machine and is pressurized to 1.65Mpa; the pressure is as follows: cooling 1.65Mpa gas nitrogen by cooler 13;
and 7: in the step 6, a part of gas nitrogen cooled by the cooler 13 enters a first channel of the plate heat exchanger 15 through a second end of the third tee joint 14 for heat exchange, liquid nitrogen subjected to heat exchange enters a gas-liquid separator 38 for gas-liquid separation after throttling through a throttle valve 36, and the liquid nitrogen subjected to gas-liquid separation enters a liquid nitrogen storage tank 3 through a pipeline between the air separation device 1 and the liquid nitrogen storage tank 3;
and 8: the other part of gas nitrogen cooled by the cooler 13 in the step 6 enters the low-temperature refrigerating device 16 through the third end of the third tee joint 14 and the second channel of the plate heat exchanger 15, and the gas nitrogen passing through the low-temperature refrigerating device 16 sequentially passes through the third channel of the plate heat exchanger 15, the expansion end 17 of the expander and the fourth channel of the plate heat exchanger 15 and enters the buffer tank 10; the gas nitrogen temperature through the second passage of the plate heat exchanger 15 is: -18 ℃, the gas nitrogen temperature through the cryogenic refrigeration unit 16 is: the temperature of the low-temperature low-pressure nitrogen is minus 180 ℃ and the pressure is 0.13MPa after the low-temperature low-pressure nitrogen is expanded through an expansion end 17 of an expander at minus 20 ℃;
and step 9: gas nitrogen generated by cold loss or pressurization in the liquid nitrogen pressurization pump 25 flows back into the liquid nitrogen storage tank 3 through the first nitrogen pipeline 26; the gas nitrogen generated in the filling process of the liquid nitrogen filling pump 27 flows back into the liquid nitrogen storage tank 3 through the second nitrogen pipeline 29; condensing the gas nitrogen into liquid nitrogen in the liquid nitrogen storage tank 3 through the steps 5 to 7, and then re-entering the liquid nitrogen storage tank 3;
the gas oxygen generated in the filling process of the liquid oxygen filling pump 30 enters the liquid oxygen storage tank 2 through an oxygen pipeline 32, and the gas oxygen is condensed into liquid oxygen in the liquid oxygen storage tank 2 through the step 2 and then enters the liquid oxygen storage tank 2 again;
and gas argon generated in the filling process of the liquid argon filling pump 33 enters the liquid argon storage tank 4 through an argon gas pipeline 35, and the gas argon is condensed into liquid argon in the liquid argon storage tank 4 through the step 3 and then enters the liquid argon storage tank 4 again.
Preferably, the gas oxygen pressure at the top gas phase outlet of the liquid oxygen storage tank 2 in the step 2 is not less than 30kpa, and the gas oxygen is vented by opening the oxygen vent valve 18 while the condenser 5 is started; in the step 3, the gas argon pressure at the top gas phase outlet of the liquid argon storage tank 4 is not less than 30kpa, and the gas argon is vented by opening an argon gas venting valve 20 while the condenser 5 is started; and (3) when the liquefaction unit in the step (5) is not started, the gas nitrogen in the condenser (5) in the step (4) after the heat exchange of the liquid nitrogen is discharged by opening a nitrogen gas discharge valve (22).
The utility model is based on the air separation system in the prior art, and carries out condensation liquefaction treatment on liquid nitrogen, liquid oxygen and liquid argon produced in the air separation system in cold loss and natural volatile gas phase; the utility model liquefies gas oxygen and gas argon based on liquid nitrogen by utilizing the boiling point difference of nitrogen, oxygen and argon, does not need to purchase a cold source, and can reduce the production cost of liquid phase products, improve the recovery rate of the liquid phase products, avoid resource waste and the stability of the liquid phase products on the basis of not changing the original air separation system; specifically, the oxygen and the argon are subjected to heat exchange and condensation through liquid nitrogen, and the gas nitrogen subjected to heat exchange is condensed through a liquefaction unit; the condensed liquid-phase product flows back into respective storage tanks to be sold; further the utility model has the characteristics of flexible operation, can be according to operating condition, security and economic type carry out the combined consideration and operate it, it particularly, can carry out the condensation liquefaction to gas oxygen alone through the liquid nitrogen, the liquid nitrogen carries out the condensation liquefaction to gas argon alone, gas nitrogen carries out the condensation liquefaction through the liquefaction unit alone, the liquid nitrogen can select direct unloading or get into the liquefaction unit and carry out the condensation liquefaction to gas oxygen and/or gas argon according to the economic nature gas nitrogen after carrying out the condensation liquefaction, the liquid nitrogen carries out the gas nitrogen after the condensation liquefaction to gas oxygen and/or gas argon and gets into the liquefaction unit jointly with the gas nitrogen in liquid nitrogen storage tank 3 and carries out the condensation liquefaction, if the form that the too high can adopt the unloading when carrying out the condensation liquefaction to gas oxygen and/or gas argon ensures entire system's security. Above-mentioned operation process is nimble controllable to actual conditions, security and economic realize carrying out the condensation liquefaction to the gas in the storage tank as the basis, not only improved liquid phase product stability and product utilization rate, can also effectively reduce the cost of enterprise's product.
In the description of the present invention, it should be noted that, unless otherwise explicitly specified or limited, the terms "connected," "connected," and the like are to be construed broadly, and may be, for example, a fixed connection, an integral connection, or a detachable connection; 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 the specific situation. The above examples are only specific illustrations of feasible embodiments of the present invention, and they are not intended to limit the scope of the present invention, and all equivalent embodiments, modifications and alterations without departing from the technical spirit of the present invention are intended to be included in the scope of the present invention.
Claims (8)
1. The utility model provides a retrieve condensation liquefaction device who diverges oxygen nitrogen argon gas, includes air separation plant (1), and air separation plant (1) links to each other its characterized in that with liquid oxygen storage tank (2), liquid nitrogen storage tank (3) and liquid argon storage tank (4) through the pipeline respectively: a top gas-phase outlet of the liquid oxygen storage tank (2) is connected with a liquid-phase return port of the liquid oxygen storage tank (2) through an oxygen liquefaction passage (6) of the condenser (5); a gas phase outlet at the top of the liquid argon storage tank (4) is connected with a liquid phase reflux port of the liquid argon storage tank (4) through an argon liquefaction channel (7) of the condenser (5); a liquid nitrogen outlet at the lower part of the liquid nitrogen storage tank (3) is connected with a shell pass of the condenser (5), a shell pass gas phase outlet of the condenser (5) is connected with the liquefaction unit, and an outlet of the liquefaction unit is connected with a third end of a first tee joint (8) arranged between the air separation device (1) and the liquid nitrogen storage tank (3); the third end of the first tee joint (8) is also connected with a shell-side liquid phase outlet of the condenser (5);
and a second tee joint (9) is arranged between the shell pass of the condenser (5) and the liquefaction unit, and the third end of the second tee joint (9) is connected with a top gas-phase outlet of the liquid nitrogen storage tank (3).
2. The condensation liquefaction device for recovering a divergent oxygen nitrogen argon gas according to claim 1, characterized in that: the liquefaction unit comprises a buffer tank (10), an outlet circulating compressor (11) of the buffer tank (10), a pressurization end (12) of an expansion machine and a cooler (13) are connected with a third tee joint (14), a second end of the third tee joint (14) is connected with a gas-liquid separator (38) through a first channel of a plate heat exchanger (15) and a throttle valve (36), and a liquid phase outlet of the gas-liquid separator (38) is connected with a pipeline between an air separation device (1) and a liquid nitrogen storage tank (3); and the second end of the second tee joint (9) is connected with an inlet of the buffer tank (10).
3. The apparatus of claim 2, wherein the condensing and liquefying apparatus for recovering a divergent oxygen-nitrogen argon gas comprises: the third end of the third tee joint (14) is connected with the inlet of a low-temperature refrigerating device (16) through a second channel of the plate heat exchanger (15), the outlet of the low-temperature refrigerating device (16) is connected with the expansion end (17) of the expander through a third channel of the plate heat exchanger (15), and the outlet of the expansion end (17) of the expander is connected with the inlet of the buffer tank (10) through a fourth channel of the plate heat exchanger (15); and the second end of the second tee joint (9) is connected with an inlet of the buffer tank (10) through a fifth channel of the plate heat exchanger (15).
4. The condensation liquefaction device for recovering a divergent oxygen nitrogen argon gas according to claim 3, characterized in that: the plate heat exchanger (15), the expansion end (17) of the expander, the throttle valve (36) and the gas-liquid separator (38) are arranged in the cold box (37).
5. The apparatus of claim 1, wherein the condensing and liquefying apparatus for recovering a divergent oxygen-nitrogen argon gas comprises: an oxygen emptying pipeline (19) with an oxygen emptying valve (18) is arranged at the inlet of the oxygen liquefaction channel (6);
an argon gas emptying pipeline (21) with an argon gas emptying valve (20) is arranged at the inlet of the argon liquefying channel (7);
and a nitrogen gas vent pipeline (23) with a nitrogen gas vent valve (22) is arranged at a shell pass gas phase outlet of the condenser (5).
6. The apparatus of claim 1, wherein the condensing and liquefying apparatus for recovering a divergent oxygen-nitrogen argon gas comprises: a fourth tee joint (24) and a liquid nitrogen booster pump (25) are sequentially arranged between a liquid nitrogen outlet at the lower part of the liquid nitrogen storage tank (3) and the shell pass of the condenser (5), and a first nitrogen pipeline (26) connected with the liquid nitrogen storage tank (3) is arranged on a gas outlet pipeline of the liquid nitrogen booster pump (25);
the third end of the fourth tee joint (24) is connected with a liquid nitrogen flushing tank car (28) through a liquid nitrogen filling pump (27), and a second nitrogen pipeline (29) connected with the liquid nitrogen storage tank (3) is arranged on a gas outlet pipeline of the liquid nitrogen filling pump (27).
7. The apparatus of claim 1, wherein the condensing and liquefying apparatus for recovering a divergent oxygen-nitrogen argon gas comprises: a liquid oxygen outlet at the lower part of the liquid oxygen storage tank (2) is connected with a liquid oxygen flushing tank car (31) through a liquid oxygen charging pump (30); an oxygen pipeline (32) connected with the liquid oxygen storage tank (2) is arranged on a gas outlet pipeline of the liquid oxygen charging pump (30).
8. The condensation liquefaction device for recovering a divergent oxygen nitrogen argon gas according to claim 1, characterized in that: a liquid argon outlet at the lower part of the liquid argon storage tank (4) is connected with a liquid argon flushing tank car (34) through a liquid argon filling pump (33); and an argon gas pipeline (35) connected with the liquid argon storage tank (4) is arranged on a gas outlet pipeline of the liquid argon filling pump (33).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202222129754.XU CN218001968U (en) | 2022-08-11 | 2022-08-11 | Condensation liquefying device for recovering diffused oxygen nitrogen argon gas |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202222129754.XU CN218001968U (en) | 2022-08-11 | 2022-08-11 | Condensation liquefying device for recovering diffused oxygen nitrogen argon gas |
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| CN218001968U true CN218001968U (en) | 2022-12-09 |
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| CN202222129754.XU Active CN218001968U (en) | 2022-08-11 | 2022-08-11 | Condensation liquefying device for recovering diffused oxygen nitrogen argon gas |
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2022
- 2022-08-11 CN CN202222129754.XU patent/CN218001968U/en active Active
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