Flue gas deoxidizing system

Abstract

Embodiments of the present application provide a flue gas deoxidation system, comprising: an oxygen absorption assembly, configured to receive flue gas and absorb oxygen in the flue gas by saturated carbon dioxide absorption liquid to form an oxygen-rich solution; a deoxidation assembly, in communication with the oxygen absorption assembly, configured to receive the oxygen-rich solution and deoxidize to form oxygen-rich gas; a drying assembly, in communication with the deoxidation assembly, configured to receive the oxygen-rich gas and dehydrate the oxygen-rich gas to form dry oxygen-rich gas; and an oxygen separation assembly, in communication with the drying assembly, configured to receive the oxygen-rich gas and separate oxygen from the oxygen-rich gas. The flue gas deoxidation system of the present application can remove oxygen from the end flue gas, thereby avoiding the oxygen in the end flue gas combining with hydrogen to form water when the end flue gas is used for ammonia synthesis reaction, and improving the efficiency and yield of the end flue gas for ammonia synthesis.

Description

TECHNICAL FIELD

[0001] Embodiments of the present application belong to the technical field of waste gas treatment, and particularly relate to a flue gas deoxidization system. BACKGROUND

[0002] After the end flue gas of a thermal power unit is deeply treated by a desulfurization and denitration dust removal process, the content of sulfur dioxide, nitrogen oxides and particulate matters in the end flue gas can be reduced to a low level, and the main components of the end flue gas are nitrogen, carbon dioxide, oxygen and water, and the typical content is 70%, 12%, 6% and 12% respectively. The end flue gas can be regarded as high-quality carbon dioxide raw material, and after carbon capture, carbon dioxide gas with a concentration of more than 99% can be obtained, which can be used for synthesizing methanol, synthesis gas and other materials; the volume ratio of nitrogen and oxygen in the end flue gas is much higher than that of air, and the end flue gas is high-quality nitrogen raw material, which can be used for synthesizing ammonia, including traditional Haber-Bosch process and emerging electro-catalytic process, but the oxygen in the end flue gas is easy to combine with hydrogen to generate water, which will significantly reduce the efficiency and amount of ammonia synthesis. SUMMARY

[0003] Embodiments of the present application aim to at least solve one of the technical problems existing in the prior art, and provide a flue gas deoxidization system.

[0004] Embodiments of the present application provide a flue gas deoxidization system, which comprises:

[0005] An oxygen absorption assembly is configured to receive flue gas and absorb oxygen in the flue gas by saturated carbon dioxide absorption liquid to form an oxygen-rich solution.

[0006] A deoxidization assembly is in communication with the oxygen absorption assembly to receive the oxygen-rich solution and perform deoxidization to form oxygen-rich gas.

[0007] A drying assembly is in communication with the deoxidization assembly to receive the oxygen-rich gas and perform dehydration on the oxygen-rich gas to form dry oxygen-rich gas.

[0008] An oxygen separation assembly is in communication with the drying assembly to receive the oxygen-rich gas and perform oxygen separation on the oxygen-rich gas.

[0009] In some embodiments of the present application, the oxygen absorption assembly comprises:

[0010] An absorption tower is provided with a gas inlet, a gas outlet and a liquid outlet, the gas inlet and the liquid outlet are arranged at the bottom of the absorption tower, the gas outlet is arranged at the top of the absorption tower, and a spraying absorption liquid is arranged in the absorption tower, which is used to absorb oxygen in the flue gas to form an oxygen-rich solution.

[0011] In some embodiments of the present invention, the oxygen inhalation assembly further includes:

[0012] An oxygen-enriched liquid tank is connected to the drain port, and the deoxygenation component is connected to the oxygen-enriched liquid tank.

[0013] In some embodiments of the present invention, the deoxygenation component includes:

[0014] An injector, which is connected to the oxygen intake assembly to receive an oxygen-enriched solution, and which is also connected to high-pressure carbon dioxide gas;

[0015] A desorber, wherein the ejector is connected to the desorber, and the desorber is connected to the drying assembly.

[0016] In some embodiments of the present invention, the drying component includes:

[0017] A first water-gas separator is connected to the deoxygenation assembly to receive oxygen-enriched gas and separate it into water and gas.

[0018] A dryer is connected to the first water-gas separator, and an oxygen separation component is connected to the dryer. The dryer is used to receive oxygen-enriched gas after water-gas separation and to dry the oxygen-enriched gas.

[0019] In some embodiments of the present invention, the drying assembly further includes a mixed gas storage tank, a compressor, a first heat exchanger, and a second water-gas separator connected in sequence. The mixed gas storage tank is connected to the first water-gas separator to receive oxygen-enriched gas after water-gas separation by the first water-gas separator. The dryer is connected to the second water-gas separator and is used to receive oxygen-enriched gas after separation by the second water-gas separator.

[0020] In some embodiments of the present invention, the oxygen separation assembly includes:

[0021] The second heat exchanger is connected to the drying assembly to receive the dried oxygen-enriched gas and cool the dried oxygen-enriched gas.

[0022] A purification tower, which is connected to the second heat exchanger, is used to receive and separate the cooled gas-liquid mixture.

[0023] An oxygen storage tank, which is connected to the purification tower, is used to receive oxygen.

[0024] A carbon dioxide storage tank, which is connected to the purification tower, is used to receive carbon dioxide.

[0025] In some embodiments of the present invention, the oxygen separation assembly further includes:

[0026] A third heat exchanger is disposed between the purification tower and the carbon dioxide storage tank, and the third heat exchanger is used to cool the flue gas before it enters the oxygen absorption assembly.

[0027] In some embodiments of the present invention, the carbon dioxide storage tank is connected to the deoxygenation assembly, and the carbon dioxide storage tank is used to provide high-pressure pure carbon dioxide gas to the deoxygenation assembly.

[0028] In some embodiments of the present invention, the flue gas deoxygenation system further includes:

[0029] An oxygen-deficient liquid tank is connected to the deoxygenation assembly to receive the oxygen-deficient liquid after deoxygenation by the deoxygenation assembly. The oxygen-deficient liquid is connected to the drying assembly to receive the oxygen-deficient liquid removed by the drying assembly. The oxygen-deficient liquid tank is connected to the oxygen absorption assembly to provide the oxygen absorption assembly with oxygen-deficient liquid as a saturated carbon dioxide absorbent.

[0030] The flue gas deoxygenation system of this invention absorbs oxygen from the terminal flue gas using an absorbent liquid in the oxygen absorption assembly. Then, a deoxygenation assembly removes the oxygen from the oxygen-enriched solution to form oxygen-enriched gas. A drying assembly then dehydrates the oxygen-enriched gas, and finally, the oxygen in the dehydrated oxygen-enriched gas is separated, thus separating the oxygen from the terminal flue gas. This flue gas deoxygenation system removes oxygen from the terminal flue gas, preventing the oxygen from combining with hydrogen to form water when the terminal flue gas is used in ammonia synthesis, thereby improving the efficiency and yield of ammonia synthesis from the terminal flue gas. Furthermore, the flue gas deoxygenation system can dry and separate the removed oxygen to obtain high-purity oxygen, which can then be used as an oxygen source for other systems. Attached Figure Description

[0031] Figure 1 This is a schematic diagram of the flue gas deoxygenation system according to an embodiment of the present invention.

[0032] The labels in the attached diagram are as follows:

[0033] 100. Flue gas deoxygenation system;

[0034] 10. Oxygen absorption assembly; 11. Absorption tower; 12. Oxygen-enriched liquid tank;

[0035] 20. Deoxygenation assembly; 21. Desorber; 22. Ejector;

[0036] 30. Drying assembly; 31. First water-gas separator; 32. Mixed gas storage tank; 33. Compressor; 34. First heat exchanger; 35. Second water-gas separator; 36. Dryer;

[0037] 40. Oxygen separation unit; 41. Second heat exchanger; 42. Purification tower; 43. Oxygen storage tank; 44. Carbon dioxide storage tank;

[0038] 50. Third heat exchanger;

[0039] 60. Oxygen-deficient liquid tank. Detailed Implementation

[0040] Exemplary embodiments of the invention will now be described in more detail with reference to the accompanying drawings. While exemplary embodiments of the invention are shown in the drawings, it should be understood that the invention can be implemented in various forms and should not be limited to the embodiments set forth herein. Rather, these embodiments are provided to enable a more thorough understanding of the invention and to fully convey the scope of the invention to those skilled in the art.

[0041] It should be understood that the terminology used herein is for the purpose of describing particular exemplary embodiments only and is not intended to be limiting. Unless the context clearly indicates otherwise, the singular forms “a,” “an,” and “described” as used herein may also include the plural forms. The terms “comprising,” “including,” “containing,” and “having” are inclusive and therefore indicate the presence of the stated features, steps, operations, elements, and / or components, but do not exclude the presence or addition of one or more other features, steps, operations, elements, components, and / or combinations thereof. The method steps, processes, and operations described herein are not construed as requiring them to be performed in a particular order described or illustrated unless the order of performance is explicitly indicated. It should also be understood that additional or alternative steps may be used.

[0042] Although terms such as first, second, third, etc., may be used in this document to describe multiple elements, components, regions, layers, and / or segments, these elements, components, regions, layers, and / or segments should not be limited by these terms. These terms may be used only to distinguish one element, component, region, layer, or segment from another. Unless the context clearly indicates otherwise, terms such as "first," "second," and other numerical terms used herein do not imply order or sequence. Therefore, the first element, component, region, layer, or segment discussed below may be referred to as the second element, component, region, layer, or segment without departing from the teachings of the exemplary embodiments.

[0043] For ease of description, spatial relative terms may be used in the text to describe the relationship of one element or feature relative to another element or feature, as shown in the figure. These relative terms include, for example, "inside," "outside," "middle," "outer," "below," "below," "above," "over," etc. Such spatial relative terms are intended to include different orientations of the device in use or operation, other than those depicted in the figure. For example, if the device in the figure is flipped, an element described as "below other elements or features" or "below other elements or features" would subsequently be oriented as "above other elements or features" or "above other elements or features." Therefore, the example term "below" can include both upper and lower orientations. The device may be otherwise oriented (rotated 90 degrees or in other directions), and the spatial relative descriptors used in the text will be interpreted accordingly.

[0044] like Figure 1 As shown, an embodiment of the present invention provides a flue gas deoxygenation system 100, which includes: an oxygen absorption component 10, a deoxygenation component 20, a drying component 30, and an oxygen separation component 40. Specifically, the oxygen absorption component 10 is used to receive flue gas and absorb oxygen in the flue gas through a saturated carbon dioxide absorbent to form an oxygen-rich solution. The deoxygenation component 20 is connected to the oxygen absorption component 10 to receive the oxygen-rich solution and deoxygenate it to form oxygen-rich gas. The drying component 30 is connected to the deoxygenation component 20 to receive the oxygen-rich gas and dehydrate it to form dry oxygen-rich gas. The oxygen separation component 40 is connected to the drying component 30 to receive the oxygen-rich gas and separate oxygen from it.

[0045] According to the flue gas deoxygenation system 100 of the present invention, oxygen in the terminal flue gas is absorbed by the absorbent in the oxygen absorption assembly 10, and then the oxygen in the oxygen-enriched solution is removed by the deoxygenation assembly 20 to form oxygen-enriched gas. The oxygen-enriched gas is then dehydrated by the drying assembly 30, and finally the oxygen in the dehydrated oxygen-enriched gas is separated, thereby separating the oxygen from the terminal flue gas. The flue gas deoxygenation system 100 of this embodiment can remove oxygen from the terminal flue gas, thereby preventing the oxygen in the terminal flue gas from combining with hydrogen to form water when used for ammonia synthesis, thus improving the efficiency and yield of ammonia synthesis from the terminal flue gas. Furthermore, the flue gas deoxygenation system 100 can also dry and separate the removed oxygen to obtain high-purity oxygen, providing an oxygen source for other systems.

[0046] In some embodiments of the present invention, the oxygen absorption assembly 10 includes an absorption tower 11, which has an air inlet, an exhaust outlet, and a liquid outlet. The air inlet and the liquid outlet are both located at the bottom of the absorption tower 11, and the exhaust outlet is located at the top of the absorption tower 11. The absorption tower 11 contains sprayed absorbent liquid. Before entering the absorption tower 11, the flue gas passes through a third heat exchanger 50, which cools the flue gas to a temperature of 25°C. The flue gas then enters the absorption tower 11 through the air inlet. Inside the absorption tower 11, saturated carbon dioxide absorbent liquid is sprayed to absorb oxygen from the flue gas. After absorbing oxygen, the carbon dioxide absorbent liquid forms an oxygen-rich saturated carbon dioxide solution, i.e., an oxygen-rich solution, which is discharged from the liquid outlet at the bottom of the absorption tower 11. After the oxygen in the flue gas is absorbed by the saturated carbon dioxide absorbent liquid, the flue gas temperature is approximately 25°C to 30°C, and the flue gas is discharged from the exhaust outlet at the top of the absorption tower 11.

[0047] In some embodiments of the present invention, the oxygen absorption assembly 10 further includes an oxygen-enriched liquid tank 12, which is connected to a drain port, and the deoxygenation assembly 20 is connected to the oxygen-enriched liquid tank 12. After the flue gas is cooled by the third heat exchanger 50, moisture will be released from the flue gas. The flue gas and the small amount of moisture released together enter the absorption tower 11 through the inlet, and the moisture enters the oxygen-enriched liquid tank 12 through the drain port. After the saturated carbon dioxide absorbent absorbs oxygen, it forms an oxygen-enriched saturated carbon dioxide solution, i.e., an oxygen-enriched solution. The oxygen-enriched solution enters the oxygen-enriched liquid tank 12 through the drain port. A small amount of moisture and the oxygen-enriched solution are stored in the oxygen-enriched liquid tank 12 to ensure a stable supply of oxygen-enriched solution to the deoxygenation assembly 20. Specifically, the oxygen content of the oxygen-enriched solution in the oxygen-enriched liquid tank 12 is above 0.5 mg / L. The oxygen-enriched liquid in the oxygen-enriched liquid tank 12 can be pumped to other processes as a water source, such as to the desulfurization system as a water source for the desulfurization system.

[0048] In some embodiments of the present invention, the deoxygenation assembly 20 includes an injector 22 and a desorber 21. The injector is a bidirectional flow sprayer. The injector 22 is connected to the oxygen-enriched liquid tank 12 of the absorption assembly. The oxygen-enriched solution in the oxygen-enriched liquid tank 12 is pumped into the liquid inlet of the injector 22 by a compression pump. High-pressure carbon dioxide gas enters the injector 22 through the gas inlet. The high-pressure carbon dioxide sprays the oxygen-enriched solution into the mixing tube in a mist form. The purity of the carbon dioxide is greater than 99%. Under the diffusion effect of the mixing tube, oxygen is released from the oxygen-enriched carbon dioxide saturated solution, forming an oxygen-deficient carbon dioxide saturated solution. The oxygen content in the oxygen-deficient carbon dioxide saturated solution is approximately 0.01 mg / L to 0.05 mg / L. The carbon dioxide in both the oxygen-enriched and oxygen-deficient solutions remains saturated. The oxygen-deficient solution, oxygen, and carbon dioxide gas enter the desorber 21. The oxygen-deficient solution enters the oxygen-deficient liquid tank from the bottom of the desorber 21, and the oxygen and carbon dioxide gas mixture enters the drying component 30 from the top of the desorber 21. That is, the oxygen-enriched gas enters the drying component 30 to dehydrate and dry the mixture.

[0049] In some embodiments of the present invention, the drying assembly 30 includes a first water-gas separator 31 and a dryer 36. Specifically, the desorber 21 of the deoxygenation assembly 20 is connected to the first water-gas separator 31, and the first water-gas separator 31 is connected to the dryer 36. Oxygen-enriched gas in the desorber 21 enters the first water-gas separator 31 through the top. The first water-gas separator 31 performs a first water-gas separation on the oxygen-enriched gas to separate some of the moisture carried in the oxygen-enriched gas. The oxygen-enriched gas after moisture separation by the first water-gas separator 31 enters the dryer 36, where the moisture in the oxygen-enriched gas is absorbed by the molecular sieve of the dryer 36. The dryer 36 passes the dried oxygen-enriched gas into the oxygen separation assembly 40 to separate the oxygen from the oxygen-enriched gas. The first water-gas separator 31 is connected to the oxygen-deficient liquid tank 60, and the first water-gas separator 31 transports some of the moisture separated from the oxygen-enriched gas to the oxygen-deficient liquid tank 60.

[0050] Furthermore, the drying assembly 30 also includes a mixed gas storage tank 32, a compressor 33, a first heat exchanger 34, and a second water-gas separator 35 connected in sequence. The mixed gas storage tank 32, the compressor 33, the first heat exchanger 34, and the second water-gas separator 35 perform a second moisture separation on the oxygen-enriched gas dried by the first water-gas separator 31, so as to further reduce the moisture content in the oxygen-enriched gas. Specifically, the first water-gas separator 31 is connected to the mixed gas storage tank 32. After separating some of the moisture from the oxygen-enriched gas, the first water-gas separator 31 transports the oxygen-enriched gas to the mixed gas storage tank 32. The oxygen-enriched gas after moisture separation by the first water-gas separator 31 is stored in the mixed gas storage tank 32 and then transported to the compressor 33. The compressor 33 pressurizes the gas to above 2.5 MPa. The compressed oxygen-enriched gas is then transported to the first heat exchanger 34, where it is cooled. The cooled oxygen-enriched gas is then transported to the second water-gas separator 35, where it performs a second water-gas separation, separating some of the moisture from the oxygen-enriched gas and transporting it to the oxygen-deficient liquid tank 60. The second water-gas separator 35 is connected to the dryer 36. The second water-gas separator 35 transports the oxygen-enriched gas after the second water-gas separation to the dryer 36 for drying. The dryer 36 reduces the moisture content of the oxygen-enriched gas to below 0.01%.

[0051] In some embodiments of the present invention, the oxygen separation assembly 40 includes: a second heat exchanger 41, a purification tower 42, an oxygen storage tank 43, and a carbon dioxide storage tank 44. Specifically, the dryer 36 of the drying assembly 30 is connected to the second heat exchanger 41, the second heat exchanger 41 is connected to the purification tower 42, and the purification tower 42 is connected to both the oxygen storage tank 43 and the carbon dioxide storage tank 44. After the oxygen-enriched gas is dried by the dryer 36 of the drying assembly 30, the moisture content of the oxygen-enriched gas is reduced to below 0.01%. The oxygen-enriched gas then enters the second heat exchanger 41 from the dryer 36. The second heat exchanger 41 cools the oxygen-enriched gas to below -25°C using liquid ammonia. The carbon dioxide gas in the oxygen-enriched gas becomes liquid carbon dioxide at -25°C, while the oxygen remains in a gaseous state. The mixture of oxygen and liquid carbon dioxide is transported to the purification tower 42. The oxygen enters the oxygen storage tank 43 from the top of the purification tower 42 for storage, while the liquid carbon dioxide enters the carbon dioxide storage tank 44 from the bottom of the purification tower 42 for storage.

[0052] In some embodiments of the present invention, the oxygen separation assembly 40 further includes a third heat exchanger 50, which is disposed between the purification tower 42 and the carbon dioxide storage tank 44. The third heat exchanger 50 uses liquid carbon dioxide to cool the flue gas. The flue gas is cooled by the third heat exchanger 50 before entering the absorption tower 11 of the oxygen absorption assembly 10, so that the temperature of the flue gas is reduced to 25°C. At the same time, the liquid carbon dioxide is heated by the high-temperature flue gas through the third heat exchanger 50, and the liquid carbon dioxide is heated to become gaseous carbon dioxide, which is then transported to the carbon dioxide storage tank 44.

[0053] In some embodiments of the present invention, the carbon dioxide storage tank 44 is connected to the deoxygenation assembly 20. Specifically, the carbon dioxide storage tank 44 is connected to the injector 22 to provide high-pressure carbon dioxide gas to the injector 22, thereby achieving resource recycling. As the desorbed gas in the desorber 21, carbon dioxide is consumed to a certain extent in the flue gas deoxygenation system. A certain amount of carbon dioxide can be replenished to the carbon dioxide storage tank 44 to maintain the normal operation of the flue gas deoxygenation system.

[0054] In some embodiments of the present invention, the flue gas deoxygenation system 100 further includes: an oxygen-deficient liquid tank 60, which is connected to the desorber 21 of the deoxygenation component 20, and the oxygen-deficient liquid is connected to both the first water-gas separator 31 and the second water-gas separator 35 of the drying component 30. The oxygen-deficient liquid tank 60 is also connected to the absorption tower 11 of the oxygen absorption component 10. The oxygen-deficient liquid tank 60 receives the oxygen-deficient liquid after deoxygenation by the deoxygenation component 20 and the oxygen-deficient liquid removed by the drying component 30. The oxygen-deficient liquid is then recycled back into the oxygen absorption component 10 as a saturated carbon dioxide absorbent for reuse.

[0055] It is understood that the above embodiments are merely exemplary implementations used to illustrate the principles of the present invention, and the present invention is not limited thereto. For those skilled in the art, various modifications and improvements can be made without departing from the spirit and essence of the present invention, and these modifications and improvements are also considered to be within the scope of protection of the present invention.

Claims

1. A flue gas deoxygenation system, characterized in that, The flue gas deoxygenation system includes: An oxygen absorption assembly is used to receive flue gas and absorb oxygen from the flue gas through a saturated carbon dioxide absorbent to form an oxygen-rich solution. A deoxygenation component, which is connected to the oxygen absorption component, is used to receive an oxygen-rich solution and deoxygenate it to form an oxygen-rich gas. A drying component, which is connected to the deoxygenation component, is used to receive the oxygen-enriched gas and dehydrate the oxygen-enriched gas to form dry oxygen-enriched gas. An oxygen separation component, which is connected to the drying component, is provided to receive the oxygen-enriched gas and perform oxygen separation on the oxygen-enriched gas. The oxygen delivery assembly includes: An absorption tower is provided, which has an air inlet, an exhaust outlet and a liquid outlet. The air inlet and the liquid outlet are located at the bottom of the absorption tower, and the exhaust outlet is located at the top of the absorption tower. The absorption tower is provided with a sprayed absorbent liquid, which is used to absorb oxygen in the flue gas to form an oxygen-rich solution. The deoxygenation assembly includes: An injector, which is connected to the oxygen intake assembly to receive an oxygen-enriched solution, and which is also connected to high-pressure carbon dioxide gas; A desorber, wherein the ejector is connected to the desorber, and the desorber is connected to the drying assembly; The oxygen separation component includes: The second heat exchanger is connected to the drying assembly to receive the dried oxygen-enriched gas and cool the dried oxygen-enriched gas. A purification tower, which is connected to the second heat exchanger, is used to receive and separate the cooled gas-liquid mixture. An oxygen storage tank, which is connected to the purification tower, is used to receive oxygen. A carbon dioxide storage tank, which is connected to the purification tower, is used to receive carbon dioxide.

2. The flue gas deoxygenation system according to claim 1, characterized in that, The oxygen delivery assembly also includes: An oxygen-enriched liquid tank is connected to the drain port, and the deoxygenation component is connected to the oxygen-enriched liquid tank.

3. The flue gas deoxygenation system according to claim 1, characterized in that the drying component comprises: A first water-gas separator is connected to the deoxygenation assembly to receive oxygen-enriched gas and separate it into water and gas. A dryer is connected to the first water-gas separator, and an oxygen separation component is connected to the dryer. The dryer is used to receive oxygen-enriched gas after water-gas separation and to dry the oxygen-enriched gas.

4. The flue gas deoxygenation system according to claim 3, characterized in that, The drying assembly further includes a mixed gas storage tank, a compressor, a first heat exchanger, and a second water-gas separator connected in sequence. The mixed gas storage tank is connected to the first water-gas separator to receive oxygen-enriched gas after water-gas separation by the first water-gas separator. The dryer is connected to the second water-gas separator and is used to receive oxygen-enriched gas after separation by the second water-gas separator.

5. The flue gas deoxygenation system according to claim 1, characterized in that, The oxygen separation assembly also includes: A third heat exchanger is disposed between the purification tower and the carbon dioxide storage tank, and the third heat exchanger is used to cool the flue gas before it enters the oxygen absorption assembly.

6. The flue gas deoxygenation system according to claim 1, characterized in that, The carbon dioxide storage tank is connected to the deoxygenation assembly, and the carbon dioxide storage tank is used to provide high-pressure carbon dioxide gas to the deoxygenation assembly.

7. The flue gas deoxygenation system according to claim 1, characterized in that, The flue gas deoxygenation system also includes: An oxygen-deficient liquid tank is connected to the deoxygenation assembly to receive the oxygen-deficient liquid after deoxygenation by the deoxygenation assembly. The oxygen-deficient liquid is connected to the drying assembly to receive the oxygen-deficient liquid removed by the drying assembly. The oxygen-deficient liquid tank is connected to the oxygen absorption assembly to provide the oxygen absorption assembly with oxygen-deficient liquid as a saturated carbon dioxide absorbent.

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