A multi-operating-condition air internal compression high-pressure oxygen air separation device

Abstract

The invention discloses a multi-condition air internal compression high-pressure oxygen air separation device, comprising an air filter, a raw air turbine compressor, an air cooling tower, a water cooling tower, an air purification unit, a booster air turbine compressor, a main heat exchanger, a distillation tower, a crude argon tower, a refined argon tower and a high-purity oxygen tower, an air boost bypass is added to the air pipeline, a booster air turbine compressor is arranged on the air boost bypass, the air boost bypass enters the main heat exchanger and reaches the lower tower, the air boost bypass enters the main heat exchanger and is provided with a middle-drawn gas expander, the middle-drawn gas expander is connected and provided with a generator I, the middle-drawn gas expander returns to the air pipeline after expansion and refrigeration and enters the lower tower, the air boost bypass enters the main heat exchanger and is provided with a liquid expander I, the liquid expander I is connected and provided with a generator II, and the liquid expander I reaches the lower tower after expansion and refrigeration. The invention achieves the separation and output of product liquid oxygen, product liquid nitrogen, product gaseous oxygen and product liquid argon, increases output and reduces energy consumption.

Description

Technical Field

[0001] The present invention relates to the technical field of air separation and gas production, and in particular to a multi-working-condition air internal compression high-pressure oxygen air separation device. Background Art

[0002] In recent years, the demand for industrial gases such as oxygen and nitrogen has increased significantly. Currently, oxygen and nitrogen, commonly used in industry, are typically produced using air separation technology. This technology utilizes the differences in boiling points of air components to separate the components of an air mixture in an air separation tower, thereby separating them into liquid oxygen, liquid nitrogen, or other gaseous products. Most current air separation units lack the ability to extract argon products, but high-purity argon is widely used in industry, particularly in aircraft manufacturing, shipbuilding, atomic energy, and machinery. It can also be used as a shielding gas in welding and electronics, and as a filler gas for lamps.

[0003] The air separation unit separates air at low temperatures to obtain products such as oxygen and nitrogen. This is essentially achieved through energy conversion. The thermal balance of the air separation unit is achieved through the refrigeration system and the heat exchange system. In the existing technology, the heat exchange system mainly uses a heat exchanger for heat exchange. Among them, the existing gas-making air separation unit has the phenomenon of poor heat exchange effect of internal compressed liquid oxygen, and cannot effectively improve the temperature difference distribution of the heat exchanger. The irreversible loss is large and the energy consumption is high. How to achieve independent load adjustment, reduce compressor linkage and high-pressure oxygen production adjustment and efficient control is currently required. Secondly, the core of the low-temperature air separation method is to use the difference in boiling points of the various components in the air to achieve the separation of gas mixtures in the distillation tower. By recovering cold through heat exchange, the various components in the air can be separated to obtain gas and liquid products. When the air separation is operated at reduced load, the compressor of the entire system of the existing technology can only be reduced to 75%. If it is lower, the operation of the air separation equipment cannot be guaranteed. Furthermore, existing air separation units utilize throttling valves to reduce pressure, which also lowers temperature. This results in a very low refrigeration effect, and the vast majority of the high-pressure air's energy is lost during throttling, increasing energy consumption for the entire compressor unit. Furthermore, the high vaporization rate of throttled liquid air negatively impacts distillation after entering the lower column. In summary, achieving pressurized high-pressure oxygen under multiple operating conditions is currently lacking, and improvements are necessary. Summary of the Invention

[0004] In order to solve the problems raised in the above background technology, the present invention provides a multi-mode air internal compression high-pressure oxygen air separation device.

[0005] To achieve the above-mentioned object, the present invention provides the following technical solution: a multi-working-mode air internal compression high-pressure oxygen air separation device, comprising an air filter, a raw air turbine compressor, an air cooling tower, a water cooling tower, an air purification unit, a booster air turbine compressor, a main heat exchanger, a distillation tower, a crude argon tower, a refined argon tower and a high-purity oxygen tower, wherein the air filter is connected to the raw air turbine compressor, the raw air turbine compressor is connected to the air cooling tower, the air cooling tower is connected to the air purification unit, the distillation tower includes an upper tower, a lower tower and a condenser evaporator, and the air purification unit The element is provided with an air pipeline, which enters the main heat exchanger and reaches the lower tower. The outputs of the lower tower and the upper tower are provided with a subcooler. The liquid air and liquid nitrogen output by the lower tower and the nitrogen, oxygen and dirty nitrogen output by the upper tower enter the subcooler. The condenser evaporator enters the subcooler and is cooled and then outputted with a liquid oxygen pipeline. The upper tower is connected to the crude argon tower. The crude argon tower is provided with a crude argon tower condenser. The output of the crude argon tower condenser is connected to the refined argon tower. The refined argon tower is provided with a liquid argon output pipeline. The high-purity oxygen tower enters the subcooler and then outputs a high-purity liquid oxygen pipeline.

[0006] An air boost bypass is added to the air pipeline, and the boost air turbine compressor is arranged on the air boost bypass. The air boost bypass enters the main heat exchanger and reaches the lower tower. The air boost bypass enters the main heat exchanger and is provided with a mid-extraction gas expander. The mid-extraction gas expander is connected to a generator I. After the mid-extraction gas expander expands and cools, it returns to the air pipeline and enters the lower tower. After the air boost bypass exits the main heat exchanger, a liquid expansion machine I is provided. The liquid expansion machine I is connected to a generator II. After the liquid expansion machine I expands and cools, it enters the lower tower.

[0007] As a preferred embodiment of the present invention, the air purification unit includes a molecular sieve adsorber I and a molecular sieve adsorber II, the molecular sieve adsorber I is connected to the molecular sieve adsorber II, and the molecular sieve adsorber I and the molecular sieve adsorber II are respectively connected to an electric heater and a muffler.

[0008] As a preferred embodiment of the present invention, the top output of the upper tower passes through the subcooler and the main heat exchanger and is outputted with a low-pressure nitrogen pipeline, the output of the lower tower enters the main heat exchanger and is outputted with a medium-pressure nitrogen pipeline, and the output of the condenser evaporator enters the main heat exchanger and is outputted with a medium-pressure oxygen pipeline.

[0009] As a preferred embodiment of the present invention, the output of the condenser evaporator is provided with a nitrogen reflux path, and the nitrogen reflux path reaches the top of the upper tower.

[0010] As a preferred embodiment of the present invention, the output of the crude argon tower condenser is connected to the upper tower, a reboiler is provided at the bottom of the refined argon tower, a refined argon reflux path is provided between the reboiler and the top of the refined argon tower, the bottom output of the lower tower passes through the subcooler to reach the reboiler, the refined argon reflux path is drawn out to connect to the top of the crude argon tower, and the top output of the refined argon tower is connected to the upper tower.

[0011] As a preferred embodiment of the present invention, the reboiler is provided with an argon reflux path, the argon reflux path is connected to the upper tower, and the argon reflux path is provided with an argon circulation pump.

[0012] As a preferred embodiment of the present invention, an oxygen pipeline is provided between the high-purity oxygen tower and the crude argon tower.

[0013] As a preferred embodiment of the present invention, a cold source supply pipeline is provided on the air pipeline, and a liquid expander II and a cooler connected in sequence are provided on the cold source supply pipeline, and the output of the liquid expander II enters the upper tower.

[0014] As a preferred embodiment of the present invention, a pipeline for air to enter the lower tower of the air pipeline is provided with a pipeline directly reaching the bottom of the high-purity oxygen tower, providing an evaporation heat source for the high-purity oxygen tower.

[0015] By adopting the above technical solution, the present invention has the following advantages compared with the prior art:

[0016] 1. The structure of the present invention is simple and reasonable. First, the raw material is air. The raw air is filtered out of dust particles by an air filter and then enters the raw air turbine compressor for compression and supercharging. It is then cooled by an air cooling tower and enters the air purification unit to remove impurities such as carbon dioxide, moisture, and hydrocarbons. The initial adsorption removal effect is good. After entering the main heat exchanger for heat exchange and cooling, it enters the lower tower of the distillation tower for distillation and purification. The air pipeline enters the main heat exchanger and reaches the lower tower. The outputs of the lower tower and the upper tower are equipped with subcoolers. The liquid air and liquid nitrogen output by the lower tower and the nitrogen, oxygen, and dirty nitrogen output by the upper tower enter the subcooler. The condenser evaporator enters the subcooler for cooling and then outputs a liquid oxygen pipeline. The product liquid oxygen can be output through the liquid oxygen pipeline. In order to tap better distillation potential and improve product extraction rate, part of the air is directly introduced into the distillation tower to participate in distillation. Since the upper tower is connected to the crude argon tower, a crude argon tower condenser is provided on the crude argon tower. The output of the crude argon tower condenser is connected to the refined argon tower. The refined argon tower is provided with a liquid argon output pipeline. The upper tower extracts crude argon gas into the crude argon tower. The crude argon gas enters the refined argon tower after distillation in the crude argon tower, and the refined liquid argon product is obtained at the bottom of the refined argon tower. The high-purity oxygen tower output is provided with a liquid oxygen pipeline, which can produce product liquid oxygen from the high-purity oxygen tower. In summary, this device can separate and output product liquid oxygen, product liquid nitrogen, product gaseous oxygen and product liquid argon, and cleverly utilizes the different boiling points of each component in the air to achieve the separation of each component in the air mixture.

[0017] 2. The air boost bypass on the air pipeline can be used to boost the pressure of the air pipeline. The air boost bypass enters the main heat exchanger equipped with a mid-extraction gas expander, which is connected to a generator I. After the mid-extraction gas expander expands and refrigerates, it returns to the air pipeline and enters the lower tower. It is mainly used to regulate and control the heat exchange between liquid oxygen and air in the main heat exchanger, recover cold energy, and vaporize and reheat to produce high-pressure oxygen, thereby efficiently improving the heat exchange effect of the internal compressed liquid oxygen, effectively improving the temperature difference distribution of the main heat exchanger, controlling the temperature difference at the hot end of the main heat exchanger to within 3°C (normally around 10°C), reducing irreversible losses, reducing energy consumption, and realizing independent load regulation. The load is reduced, the compressor linkage is reduced, the high-pressure oxygen output is regulated and efficiently controlled, and the refrigeration of the mid-extraction gas expander is used as the cooling capacity supplement of the main heat exchanger, so that the load can continue to be reduced (50-75%) without emptying and the air separation unit can operate normally. When reducing the load, the compressor can only be reduced to 75%, and it cannot operate if it is lower, ensuring the operation of the air separation unit. The mid-extraction gas expander adopts generator I braking to recover electrical energy, which can avoid the waste of air emptying and convert it into cooling capacity and electrical energy recovery, thereby increasing the liquid refrigeration capacity, and can expand the load adjustment range (75%-100%) to (50-100%), so that the operation of the air separation unit will not be affected when reducing the load.

[0018] 3. The air is pressurized and bypassed into the main heat exchanger, where a liquid expander I is installed. The liquid expander I is connected to a generator II. After the liquid expander I is expanded and cooled, it reaches the lower tower. The liquid expander I is braked by the generator II to recover electrical energy. After the liquid expander I expands the liquid air, it enters the lower tower to participate in distillation, which reduces the cooling effect of the traditional throttle valve and improves the refrigeration efficiency by 1-10%. The isentropic process can recover more energy than the isenthalpic process, greatly reducing energy consumption. The liquid air vaporization rate at the outlet of the liquid expander I is low, which is conducive to distillation, increases production capacity, and can increase the liquid output of the equipment.

[0019] 4. In summary, after adopting the above structure, the air separation unit can pressurize high-pressure oxygen under multiple working conditions, and its functionality is greatly improved. BRIEF DESCRIPTION OF THE DRAWINGS

[0020] The accompanying drawings are used to provide a further understanding of the present invention and constitute a part of the specification. Together with the embodiments of the present invention, they are used to explain the present invention and do not constitute a limitation of the present invention. In the accompanying drawings:

[0021] Figure 1 It is a schematic diagram of the principle of the present invention;

[0022] In the figure: 1. Air filter; 2. Raw air turbine compressor; 3. Air cooling tower; 4. Water cooling tower; 5. Booster air turbine compressor; 6. Main heat exchanger; 7. Distillation tower; 8. Crude argon tower; 9. Refined argon tower; 10. High-purity oxygen tower; 11. Upper tower; 12. Lower tower; 13. Condenser evaporator; 14. Air pipeline; 15. Subcooler; 16. Liquid oxygen pipeline; 17. Crude argon tower condenser; 18. Liquid argon output pipeline; 19. High-purity liquid oxygen pipeline; 20. Air boost bypass; 21. Mid-extraction gas expander; 22. Generator I; 23. Liquid expander I; 24. Generator II; 25. Molecular sieve adsorber I; 26. Molecular sieve adsorber II; 27. Electric heater; 28. Muffler; 29. ​​Low-pressure nitrogen pipeline; 30. Medium-pressure nitrogen pipeline; 31. Medium-pressure oxygen pipeline; 32. Nitrogen reflux line; 33. Reboiler; 34. Refined argon reflux line; 35. Argon reflux line; 36. Argon circulation pump; 37. Oxygen pipeline; 38. Cold source supply pipeline; 39. Liquid expander II; 40. Cooler; 41. Pipeline directly to the bottom of the high-purity oxygen tower. DETAILED DESCRIPTION

[0023] In order to make the technical means, creative features, objectives and effects achieved by the present invention easier to understand, the present invention is further described below in conjunction with specific implementation methods.

[0024] See also Figure 1 The present invention provides a technical solution: a multi-working-mode air internal compression high-pressure oxygen air separation device, comprising an air filter 1, a raw air turbine compressor 2, an air cooling tower 3, a water cooling tower 4, an air purification unit, a booster air turbine compressor 5, a main heat exchanger 6, a distillation tower 7, a crude argon tower 8, a refined argon tower 9 and a high-purity oxygen tower 10, the air filter 1 is connected to the raw air turbine compressor 2, the raw air turbine compressor 2 is connected to the air cooling tower 3, the air cooling tower 3 is connected to the air purification unit, the distillation tower 7 includes an upper tower 11, a lower tower 12 and a condenser evaporator 13, and the air purification unit is provided with an air pipeline 1 4. The air pipeline 14 enters the main heat exchanger 6 and reaches the lower tower 12. The outputs of the lower tower 12 and the upper tower 11 are provided with a subcooler 15. The liquid air and liquid nitrogen outputted from the lower tower 12 and the nitrogen, oxygen and dirty nitrogen outputted from the upper tower 11 enter the subcooler 15. The condenser evaporator 13 enters the subcooler 15 and is cooled, and then the output is provided with a liquid oxygen pipeline 16. The upper tower 11 is connected to the crude argon tower 8. The crude argon tower 8 is provided with a crude argon tower condenser 17. The output of the crude argon tower condenser 17 is connected to the refined argon tower 9. The refined argon tower 9 is provided with a liquid argon output pipeline 18. The high-purity oxygen tower 10 enters the subcooler 15 and the output is provided with a high-purity liquid oxygen pipeline 19.

[0025] An air boost bypass 20 is added to the air pipeline 14, and the boost air turbine compressor 5 is arranged on the air boost bypass 20. The air boost bypass 20 enters the main heat exchanger 6 and reaches the lower tower 12. The air boost bypass 20 enters the main heat exchanger 6 and is provided with a mid-extraction gas expander 21. The mid-extraction gas expander 21 is connected to a generator I22. After the mid-extraction gas expander 21 expands and cools, it returns to the air pipeline 14 and enters the lower tower 12. After the air boost bypass 20 exits the main heat exchanger 6, a liquid expansion machine I23 is provided. The liquid expansion machine I23 is connected to a generator II24. The liquid expansion machine I23 expands and cools and enters the lower tower 12.

[0026] In this embodiment, the present invention has a simple and reasonable structure. First, the raw material is air. The raw air is filtered out of dust particles by the air filter 1 and then enters the raw air turbine compressor 2 for compression and supercharging. It is then cooled by the air cooling tower 3 and enters the air purification unit to remove impurities such as carbon dioxide, moisture, and hydrocarbons. The initial adsorption removal effect is good. After entering the main heat exchanger 6 for heat exchange and cooling, it enters the lower tower 12 of the distillation tower 7 for distillation and purification. The air pipeline 14 enters the main heat exchanger 6 to reach the lower tower 12. The outputs of the lower tower 12 and the upper tower 11 are provided with a subcooler 15. The liquid air and liquid nitrogen output by the lower tower 12 and the nitrogen, oxygen, and dirty nitrogen output by the upper tower 11 enter the subcooler 15. The condenser evaporator 13 enters the subcooler 15 and is cooled and then outputted with a liquid oxygen pipeline 16. The liquid oxygen pipeline 16 can be used for Product liquid oxygen is output. In order to tap better distillation potential and improve product extraction rate, part of the air is directly introduced into the distillation tower to participate in distillation. Since the upper tower 11 is connected to the crude argon tower 8, the crude argon tower 8 is provided with a crude argon tower condenser 17. The output of the crude argon tower condenser 17 is connected to the refined argon tower 9. The refined argon tower 9 is provided with a liquid argon output pipeline 18. The upper tower 11 extracts crude argon gas into the crude argon tower 8. The crude argon gas enters the refined argon tower 9 after distillation in the crude argon tower 8. The refined liquid argon product is obtained at the bottom of the refined argon tower 9. The high-purity oxygen tower 10 output is provided with a liquid oxygen pipeline 16, which can produce product liquid oxygen from the high-purity oxygen tower 10. In summary, this device can separate and output product liquid oxygen, product liquid nitrogen, product gaseous oxygen and product liquid argon, and cleverly utilizes the different boiling points of each component in the air to achieve the separation of each component in the air mixture.

[0027] The air boost bypass 20 on the air pipeline 14 can be used to boost the pressure of the air pipeline 14. The air boost bypass 20 enters the main heat exchanger 6, which is equipped with a mid-extraction gas expander 21. The mid-extraction gas expander 21 is connected to a generator 122. After expansion and refrigeration, the mid-extraction gas expander 21 returns to the air pipeline 14 and enters the lower tower 12. It is mainly used to regulate and control the heat exchange between liquid oxygen and air in the main heat exchanger 6, recover cold energy, and vaporize and reheat to produce high-pressure oxygen, thereby efficiently improving the heat exchange effect of the internal compressed liquid oxygen, effectively improving the temperature difference distribution of the main heat exchanger 6, controlling the temperature difference at the hot end of the main heat exchanger 6 to be within 3°C (conventionally around 10°C), reducing irreversible losses, and reducing energy consumption. , it can realize independent load adjustment, reduce compressor linkage, and efficiently control the high-pressure oxygen production adjustment. The refrigeration of the intermediate gas expander 21 is used as the cooling capacity supplement of the main heat exchanger 6, so that the load can continue to be reduced (50-75%) without emptying and the air separation unit can operate normally. When reducing the load, the compressor can only be reduced to 75%, and it cannot operate if it is lower, ensuring the operation of the air separation unit. The intermediate gas expander 21 adopts the generator I22 to brake and recover electrical energy, which can avoid the waste of air emptying and convert it into cooling capacity and electrical energy recovery, thereby increasing the liquid refrigeration capacity, and can realize the expansion of the load adjustment range (75%-100%) to (50-100%), and the operation of the air separation unit can be affected when reducing the load.

[0028] The air boost bypass 20 enters the main heat exchanger 6, which is equipped with a liquid expander I23. The liquid expander I23 is connected to a generator II24. After the liquid expander I23 expands and cools, it reaches the lower tower 12. The liquid expander I23 is braked by the generator II24 to recover electrical energy. After the liquid expander I23 expands the liquid air, it enters the lower tower 12 to participate in distillation, reducing the cooling effect of the traditional throttle valve and improving the refrigeration efficiency by 1-10%. The isentropic process can recover more energy than the isenthalpic process, greatly reducing energy consumption. The liquid air vaporization rate at the outlet of the liquid expander I23 is low, which is conducive to distillation, increasing production capacity, and increasing the liquid output of the equipment.

[0029] In summary, after adopting the above structure, the air separation unit can pressurize high-pressure oxygen under multiple working conditions, and its functionality is greatly improved.

[0030] Specifically, the air filter 1 is a self-cleaning filter, capable of self-cleaning after filtration, achieving excellent filtration results. The condenser evaporator 13 primarily functions as a refrigeration unit, condensing gas into liquid by absorbing heat. Prior to adsorption in the air purification unit, the installation and connection structure of the air cooling tower 3 and the water cooling tower 4 are conventional, resulting in excellent air pre-cooling.

[0031] Furthermore, the air purification unit includes a molecular sieve adsorber I25 and a molecular sieve adsorber II26, the molecular sieve adsorber I25 is connected to the molecular sieve adsorber II26, and the molecular sieve adsorber I25 and the molecular sieve adsorber II26 are respectively connected to an electric heater 27 and a muffler 28.

[0032] In this embodiment, the molecular sieve adsorber I25 and the molecular sieve adsorber II26 are operated alternately to remove impurities such as carbon dioxide, moisture, and hydrocarbons in the air purification unit. The electric heater 27 can heat the regenerated gas to facilitate subsequent removal of impurities, and the muffler 28 can reduce working noise.

[0033] Furthermore, the top output of the upper tower 11 passes through the subcooler 15 and the main heat exchanger 6 and is outputted with a low-pressure nitrogen pipeline 29, the output of the lower tower 12 enters the main heat exchanger 6 and is outputted with a medium-pressure nitrogen pipeline 30, and the output of the condenser evaporator 13 enters the main heat exchanger 6 and is outputted with a medium-pressure oxygen pipeline 31.

[0034] In this embodiment, the above structure can produce low-pressure nitrogen, medium-pressure nitrogen and medium-pressure oxygen.

[0035] Furthermore, a nitrogen reflux line 32 is provided at the output of the condenser evaporator 13 , and the nitrogen reflux line 32 reaches the top of the upper tower 11 .

[0036] In this embodiment, by providing the nitrogen reflux line 32, the condenser evaporator 13 condenses the liquid nitrogen and then returns it to the upper tower 11 through the nitrogen reflux line 32 as reflux liquid to participate in the distillation. The reflux liquid can be recovered through heat, thereby reducing energy consumption, lowering production costs, and improving economic benefits.

[0037] Furthermore, the output of the crude argon tower condenser 17 is connected to the upper tower 11, a reboiler 33 is provided at the bottom of the refined argon tower 9, and a refined argon reflux line 34 is provided between the reboiler 33 and the top of the refined argon tower 9. The bottom output of the lower tower 12 passes through the subcooler 15 to reach the reboiler 33, and the refined argon reflux line 34 is drawn out to connect to the top of the crude argon tower 8, and the top output of the refined argon tower 9 is connected to the upper tower 11.

[0038] In this embodiment, the crude argon gas extracted from the upper tower 11 enters the bottom of the crude argon tower 8, rises from the bottom to the top of the crude argon tower 8, and then enters the crude argon tower 8. During the process of rising from the bottom to the top of the crude argon tower 8, the oxygen content in the crude liquid argon fraction becomes lower and lower. Process argon is obtained at the top of the crude argon tower 8, and the process argon is transported to the middle of the refined argon tower 9 for rectification. Nitrogen is removed in the refined argon tower 9, and pure liquid argon is obtained at the bottom of the refined argon tower 9 through the reboiler 33. The refined argon reflux line 34 can provide reflux liquid for recovering cold energy, thereby achieving energy saving. The output of the reboiler 33 passes through the subcooler 15 and reaches the bottom of the lower tower 12, which can recover the cold energy of argon for the lower tower 12 and increase the product output of liquid oxygen and liquid nitrogen. A path of the refined argon reflux line 34 is extracted and connected to the top of the crude argon tower 8, thereby also increasing the recovered cold energy for the crude argon tower 8. The output from the top of the refined argon tower 9 is connected to the upper tower 11, also recovering cold energy for the upper tower 11.

[0039] Furthermore, an argon reflux line 35 is provided on the reboiler 33 , the argon reflux line 35 is connected to the upper tower 11 , and an argon circulation pump 36 is provided on the argon reflux line 35 .

[0040] In this embodiment, the reflux through the argon reflux line 35 can increase the cooling capacity of the upper tower 11, and the argon circulation pump 36 plays a role in circulating and pressurizing.

[0041] Furthermore, an oxygen pipeline 37 is provided between the high-purity oxygen tower 10 and the crude argon tower 8 .

[0042] In this embodiment, the output of the oxygen pipeline 37 provides a cold source for the crude argon column 8 .

[0043] Furthermore, a cold source supply pipeline 38 is provided on the air pipeline 14 , and a liquid expander II 39 and a cooler 40 connected in sequence are provided on the cold source supply pipeline 38 , and the output of the liquid expander II 39 enters the upper tower 11 .

[0044] In this embodiment, the cold source providing pipeline 38 can provide a cold source, and the liquid expander II 39 can play a refrigeration role to provide a cold source for the distillation tower 7.

[0045] Furthermore, a pipeline 41 directly reaching the bottom of the high-purity oxygen tower is provided on the air pipeline 14 for the air to enter the lower tower 12, so as to provide an evaporation heat source for the high-purity oxygen tower 10.

[0046] In this embodiment, the air pipeline 14 provides air to the high purity oxygen tower 10 for use by the high purity oxygen tower 10 and provides an evaporation heat source for the high purity oxygen tower 10 .

[0047] It should be noted that, in this document, relational terms such as first and second, etc., are used only to distinguish one entity or operation from another entity or operation, and do not necessarily require or imply any actual relationship or order between these entities or operations. Moreover, the terms "comprises," "comprising," or any other variations thereof are intended to cover non-exclusive inclusion, such that a process, method, article, or apparatus that includes a list of elements includes not only those elements but also other elements not explicitly listed, or elements inherent to such process, method, article, or apparatus.

[0048] Finally, it should be noted that the above descriptions are merely preferred embodiments of the present invention and are not intended to limit the present invention. Although the present invention has been described in detail with reference to the aforementioned embodiments, those skilled in the art will be able to modify the technical solutions described in the aforementioned embodiments or substitute equivalents for some of the technical features. Any modifications, equivalent substitutions, and improvements made within the spirit and principles of the present invention shall be included within the scope of protection of the present invention.

Claims

1. A multi-mode air internal compression high-pressure oxygen air separation device, characterized in that: The invention comprises an air filter, a raw air turbine compressor, an air cooling tower, a water cooling tower, an air purification unit, a booster air turbine compressor, a main heat exchanger, a distillation tower, a crude argon tower, a refined argon tower and a high purity oxygen tower, wherein the air filter is connected to the raw air turbine compressor, the raw air turbine compressor is connected to the air cooling tower, the air cooling tower is connected to the air purification unit, the distillation tower comprises an upper tower, a lower tower and a condenser evaporator, the air purification unit is provided with an air pipeline, and the air pipeline enters the main heat exchanger. The heat reaches the lower tower, the lower tower and the upper tower output are provided with a subcooler, the liquid air and liquid nitrogen output by the lower tower and the nitrogen, oxygen and dirty nitrogen output by the upper tower enter the subcooler, the condenser evaporator enters the subcooler and is cooled and then outputted with a liquid oxygen pipeline, the upper tower is connected with the crude argon tower, the crude argon tower is provided with a crude argon tower condenser, the output of the crude argon tower condenser is connected with the refined argon tower, the refined argon tower is provided with a liquid argon output pipeline, the high-purity oxygen tower enters the subcooler and then outputs with a high-purity liquid oxygen pipeline; An air boost bypass is additionally provided on the air pipeline, and the boost air turbine compressor is arranged on the air boost bypass. The air boost bypass enters the main heat exchanger and reaches the lower tower. The air boost bypass enters the main heat exchanger and is provided with a middle-extraction gas expander. The middle-extraction gas expander is connected to a generator I. After the middle-extraction gas expander expands and cools, it returns to the air pipeline and enters the lower tower. After the air boost bypass exits the main heat exchanger, a liquid expansion machine I is provided. The liquid expansion machine I is connected to a generator II. After the liquid expansion machine I expands and cools, it enters the lower tower.

2. The multi-mode air internal compression high-pressure oxygen air separation device according to claim 1, characterized in that: The air purification unit comprises a molecular sieve adsorber I and a molecular sieve adsorber II, wherein the molecular sieve adsorber I is connected to the molecular sieve adsorber II, and the molecular sieve adsorber I and the molecular sieve adsorber II are respectively connected to an electric heater and a muffler.

3. The multi-mode air internal compression high-pressure oxygen air separation device according to claim 1, characterized in that: The top output of the upper tower passes through the subcooler and the main heat exchanger and is outputted with a low-pressure nitrogen pipeline, the output of the lower tower enters the main heat exchanger and is outputted with a medium-pressure nitrogen pipeline, and the output of the condenser evaporator enters the main heat exchanger and is outputted with a medium-pressure oxygen pipeline.

4. The multi-mode air internal compression high-pressure oxygen air separation device according to claim 1, characterized in that: The condenser evaporator output is provided with a nitrogen reflux path, and the nitrogen reflux path reaches the top of the upper tower.

5. The multi-mode air internal compression high-pressure oxygen air separation device according to claim 1, characterized in that: The output of the crude argon tower condenser is connected to the upper tower, a reboiler is provided at the bottom of the refined argon tower, a refined argon reflux path is provided between the reboiler and the top of the refined argon tower, the bottom output of the lower tower reaches the reboiler through a subcooler, the refined argon reflux path is drawn out to connect to the top of the crude argon tower, and the top output of the refined argon tower is connected to the upper tower.

6. The multi-mode air internal compression high-pressure oxygen air separation device according to claim 5, characterized in that: The reboiler is provided with an argon reflux path, the argon reflux path is connected to the upper tower, and an argon circulation pump is provided on the argon reflux path.

7. The multi-mode air internal compression high-pressure oxygen air separation device according to claim 1, characterized in that: An oxygen pipeline is arranged between the high purity oxygen tower and the crude argon tower.

8. The multi-mode air internal compression high-pressure oxygen air separation device according to claim 1, characterized in that: The air pipeline is provided with a cold source supply pipeline, and the cold source supply pipeline is provided with a liquid expander II and a cooler connected in sequence, and the output of the liquid expander II enters the upper tower.

9. The multi-mode air internal compression high-pressure oxygen air separation device according to claim 1, characterized in that: A pipeline directly reaching the bottom of the high-purity oxygen tower is arranged on the air pipeline for the air to enter the lower tower, so as to provide an evaporation heat source for the high-purity oxygen tower.

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