CN215161044U - High-purity carbon dioxide gas purification device - Google Patents
High-purity carbon dioxide gas purification device Download PDFInfo
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- CN215161044U CN215161044U CN202121042954.0U CN202121042954U CN215161044U CN 215161044 U CN215161044 U CN 215161044U CN 202121042954 U CN202121042954 U CN 202121042954U CN 215161044 U CN215161044 U CN 215161044U
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Abstract
The utility model belongs to the technical field of gas separation, specifically be high-purity carbon dioxide gas purification device. The utility model adopts the pressure swing adsorption technology of the carbon dioxide adsorbent of the equilibrium adsorption mechanism, obtains high-purity carbon dioxide from the adsorption phase under lower pressure, and couples pressurization, refrigeration, dewatering and carbon dioxide liquefaction to obtain high-purity liquid carbon dioxide as product gas; the device comprises compression equipment provided with pressure feed gas, a pressure swing adsorption separation device filled with a carbon dioxide adsorbent, a product gas buffer tank, a waste gas buffer tank, a supercharger, a refrigerant heat exchanger, a necessary connecting pipeline and a control valve for product gas aftertreatment, and a control assembly for controlling and operating each component. Typical pressure swing adsorption devices are two groups of adsorption towers, which form symmetrically running adsorption components; the utility model discloses can follow and purify the carbon dioxide gas that obtains 60 ~ 99.9% in the carbon dioxide gas mixture that contains about 15%.
Description
Technical Field
The utility model belongs to the technical field of gas separation, concretely relates to low partial pressure carbon dioxide gas mixture purification device.
Background
Pressure Swing Adsorption (PSA) is an important and widely used gas separation process, such as pressure swing adsorption drying, pressure swing adsorption oxygen production, nitrogen production, etc., and generally, different adsorbents are used to separate different mixed gases to obtain desired components based on pressure swing adsorption with equilibrium adsorption or kinetic separation characteristics.
Carbon dioxide (CO)2) Is the main greenhouse gas, CO, responsible for global climate change2The capture, utilization and sequestration of (a) has become one of the hot issues of international social concern. The industrial fields of steel making, cement, chemical industry (such as ammonia synthesis, hydrogen production, natural gas purification) and the like all have a large amount of CO2And (5) discharging. At present, China generates CO in flue gas generated by combustion2The recovery measure is to use chemical absorption and temperature-changing regeneration method to recover CO in flue gas2Separating, and compressing, liquefying, and refining to obtain industrial grade or food grade CO2The product, the system technology is complicated, the investment is large, the equipment occupies a large area, especially a miniaturized system, and no simple, feasible and effective solution is provided.
SUMMERY OF THE UTILITY MODEL
In view of the above circumstances, the flue gas generated in the combustion chemical reaction process usually contains nitrogen, oxygen and moisture in the background gas, and is a carbon dioxide mixed gas containing nitrogen, oxygen and moisture, the utility model provides a nitrogen, oxygen and moisture in the flue gas are removed by non-cryogenic air separation technical means, thereby obtaining a high-purity carbon dioxide device;
the utility model provides a purification device of high-purity carbon dioxide adopts the pressure swing adsorption technique based on the carbon dioxide adsorbent of balanced adsorption mechanism, and the self-absorption phase obtains high-purity carbon dioxide under lower pressure to coupling pressure boost, refrigeration, dewatering and carbon dioxide liquefaction, regard as product gas with the liquid carbon dioxide of high-purity, wherein:
the pressure swing adsorption technology based on the equilibrium adsorption mechanism is characterized in that a carbon dioxide adsorbent is filled in an adsorption bed layer, the adsorbent has stronger adsorption capacity on moisture and carbon dioxide in raw material gas relative to nitrogen and oxygen components, and high-purity carbon dioxide and water vapor mixed gas is obtained through desorption after the adsorption saturation of the bed layer;
in addition, the gas phase component in the bed layer is replaced by the carbon dioxide product gas with higher purity through circulating feeding, and the mixed gas of the carbon dioxide and the water vapor with higher purity can be obtained through desorption after the adsorption saturation of the bed layer;
in addition, in the utility model, a gas recovery loop is designed between two or more groups of beds which run symmetrically, so as to reduce the loss of the target gas to the maximum extent and improve the recovery rate;
moreover, in the utility model, at least one part of the waste gas generated in the adsorption and separation process flows back to the symmetrical separation bed layer, which is beneficial to the boosting process of the symmetrical separation bed layer and the reduction of the power consumption in the desorption process, and improves the recovery rate of the system;
moreover, in the utility model, at least a part of the product gas will flow back to the feed end of the adsorption bed layer to replace impure gas in the gas phase;
moreover, in the utility model, by adopting the purification process, the carbon dioxide mixed gas containing about 15% of typical flue gas is preferably purified to obtain the carbon dioxide purity of 60-99.9%, and more preferably to obtain the carbon dioxide purity of 60-85%;
furthermore, in the utility model, the product carbon dioxide gas pressurization process of follow-up coupling adopts two-stage refrigeration to reach the purpose of dispelling moisture and liquefied carbon dioxide respectively, wherein, preferably dispel moisture wherein with first-stage refrigeration (typical, can the freeze dryer) under 3 ~ 7.5MPa pressure to reach the technology purpose of ordinary pressure dew point-65 ℃, and is different from the dehydration process that the prior art mostly carries out the feed gas at the front end at this station, the utility model discloses combine the required pressure boost process of carbon dioxide itself to dispel moisture at this station;
and, the utility model discloses in, the pressurized process of the product carbon dioxide gas of follow-up coupling adopts the two-stage refrigeration in order to reach the purpose of dispelling moisture and liquefied carbon dioxide respectively, wherein, preferably under 3 ~ 7.5MPa pressure, select the process purpose that the liquefaction is accomplished to the gas mixture of 60 ~ 85% carbon dioxide purity that the purification system obtained under 1 ~ 15 ℃, 3 ~ 7.5MPa condition with second grade refrigeration (typical, can the refrigerant water heat transfer), and noncondensable gas wherein then gets rid of the system.
Based on the above principle, the utility model provides a purification device of high-purity carbon dioxide, include:
(1) at least one compression device for providing necessary raw gas with pressure, preferably but not necessarily comprising a device (not shown in the figure) required for pretreatment, for example, the mixed gas of carbon dioxide containing oxygen, nitrogen and water has the pressure of 15-100 kpa (gauge pressure) and does not need to be matched;
(2) at least one set of pressure swing adsorption device in the known technology, which at least comprises an adsorption tower, wherein a carbon dioxide adsorbent is arranged in the adsorption tower; typically, 13X or other modified regenerable carbon dioxide sorbents with equilibrium adsorption characteristics are used. One or more of molecular sieves for adsorbing water, such as activated alumina, silica gel and the like, can be compositely filled at the gas inlet end of the raw gas to remove impurity gases, such as water, total hydrocarbon and the like, contained in the mixed gas; the system also comprises an air inlet valve for raw material gas to enter each adsorption tower and a necessary connecting pipeline thereof, an exhaust valve for waste gas to enter the waste gas buffer tank and a necessary connecting pipeline thereof, and a gas production valve for product gas to enter the product gas buffer tank and a necessary connecting pipeline thereof; control valves for fluid exchange between symmetrically operating towers and necessary pipelines thereof for regulating and cutting off gas flow between the adsorption towers; the product gas enters the gas inlet valve of each adsorption tower and necessary pipelines thereof;
(3) at least one waste gas buffer tank connected with the exhaust end of each separator through a control valve and a necessary connecting pipeline for receiving waste gas from the separator and sending the temporarily stored waste gas into the separator which is in the process of pre-charging at the exhaust end of the separator;
(4) at least one product gas buffer tank, which is connected with the feed end of each separator through a control valve and a necessary connecting pipeline thereof by a desorption vacuum pump, is used for receiving the product gas from the separator, and sending the product gas in the product buffer tank into the gas inlet end of the separator through the control valve and the necessary connecting pipeline thereof to repressurize the separator which is in the adsorption process;
(5) at least one product gas booster for boosting the product gas in the product gas buffer tank to a predetermined pressure;
(6) at least one refrigerant heat exchanger and a filter, the gas is cooled, the moisture in the gas is condensed into liquid state, and the liquid state is removed through the filter and discharged out of the system;
(7) the at least one heat exchanger is used for cooling the carbon dioxide mixed gas from which the moisture is removed to a liquefaction triple point of the mixed gas, liquefying the carbon dioxide in the mixed gas as a product and outputting the product, and discharging the non-condensable gas out of the system;
(8) and the complete set of control components is used for carrying out necessary operation control on the valves on the loop and carrying out necessary control operation on equipment such as compression equipment, a vacuum pump, refrigeration equipment, a heat exchanger and the like.
The utility model discloses can be used for adopting one kind, multiple adsorbent to separate out the gas that is difficult to be adsorbed from the gas of difficult absorption/seeing through, easily adsorb/see through the component, perhaps difficult absorption/see through the component, all can regard as required product gas alone or simultaneously. The utility model discloses the priority is applied to the PSA process based on balanced adsorption theory rather than dynamics separation theory, nevertheless does not get rid of the PSA process based on dynamics separation theory and can adopt the utility model discloses in order to realize the utility model discloses the purpose. The basic principles disclosed can be applied to many other separation applications. Through the utility model discloses, can realize that the typical example of separation includes:
by selective adsorption of N2To recover N from air2；
By selective adsorption of O2For recovering O from the air2；
Enriching CO from the carbon monoxide mixed gas by using an adsorbing material for selectively adsorbing CO;
by selective adsorption of CO2For enriching CO from carbon dioxide gas mixture2；
Realization of CO2/CH4Separation of, CO2/N2Separation of (A) from (B), H2/N2Separation of olefins/alkanes, etc.
From containing O2Separation of O from a gas mixture of Ar (e.g. obtained by separation of air by pressure swing adsorption coupled membrane separation)2Or Ar;
any combination of one or more suitable adsorbents may also be used for separation, for example, CaA zeolite, LiX zeolite, or any other specific separation material to recover oxygen or nitrogen; gases that are difficult to adsorb/permeate are enriched from the non-feed end while components that are more readily selectively adsorbed/permeate are enriched from the other end.
In the utility model, the product gas refers to the gas which is difficult to be adsorbed by the adsorbent, for example, for the nitrogen adsorbent, nitrogen is easy to be adsorbed, oxygen and argon are difficult to be adsorbed, for the oxygen adsorbent, oxygen is easy to be adsorbed, and argon is difficult to be adsorbed;
in the present invention, the waste gas refers to gas that is relatively easily adsorbed by the adsorbent, such as nitrogen, oxygen, etc., which is relatively easily adsorbed by the nitrogen adsorbent and the oxygen adsorbent.
The present invention relates to an oxygen generation system, and more particularly to an oxygen generation system, wherein the oxygen generation system is composed of 13X molecular sieves, activated alumina, silica gel, etc. the nitrogen adsorbents such as CaA, CaX, NaX, LiX, etc. are used for pressure swing adsorption of dry molecular sieves such as 13X, activated alumina, silica gel, etc. and are usually used in the conventional PSA method for producing oxygen by air flow.
The adsorption tower, also called as adsorber, adsorption bed, separator, of the utility model refers to a container filled with at least one adsorbent, which has stronger adsorption capacity to the components that are easy to be adsorbed in the mixed gas.
In the present invention, the terms of Pressure Swing Adsorption, Adsorption separation, PSA, etc. are known to those skilled in the art, and these methods refer to not only PSA methods, but also methods similar thereto, such as Vacuum Swing Adsorption (VSA) or Mixed Pressure Swing Adsorption (MPSA), etc., which are understood in a broader sense, that is, for the Adsorption Pressure of the periodic cycle, a higher Pressure is a higher Pressure relative to the desorption step, which may include a Pressure greater than or equal to atmospheric Pressure, and for the desorption Pressure of the periodic cycle, a lower Pressure is a lower Pressure relative to the Adsorption step, which includes a Pressure less than or equal to atmospheric Pressure.
The above method and apparatus of the present invention do not exclude the use of multiple parallel adsorption separators for separation, and the air flow form of the adsorption separators can use axial flow, radial flow, lateral flow or other forms. Those skilled in the art will appreciate that even three or more of various types of separators may be used for separation, by providing the necessary additional lines and switching valves.
The product gas buffer vessel, such as described in the known art, may be filled with the necessary packing to achieve a more economical buffer volume.
The above method and device of the utility model, at feed gas entry, middle process and product gas outlet end, can set up necessary gaseous check out test set, install necessary pressure detection, dew point detection, purity check out test set on separator, buffer tank to form a system that moves according to required pressure and purity completely, and give in control by the intelligent control procedure. The method is not difficult to realize in the technical field, and experienced technicians know that the debugging process of the equipment is almost the process from system self-adaptation to stability, and in the fault judgment, a control program gives more sufficient information to maintenance and repair personnel and even directly specifies a fault point.
Regarding liquefaction of carbon dioxide as a product gas, basic physical property data of carbon dioxide are shown in table 1 below:
TABLE 1 basic physical data of carbon dioxide
Obviously, the temperature is lower, and the required pressure of gas-liquid phase transition is less, but the realization of temperature, pressure all need consume a large amount of refrigeration, compression energy, the utility model discloses preferred adoption refrigerant water is the cold source, and the low-cost acquisition of relatively easy is usually, for example, adopts typical last water temperature 3 ℃ (if can be lower, then better), return water temperature 10 ℃ to liquefy, but furthest's reduction liquefaction's compression consumption, the efficiency of low temperature liquefaction, storage is taken into comprehensive consideration.
In addition, as shown in the following table 2, at 10 ℃, the pressure required by the condensation of carbon dioxide is respectively 15MPa and 6.5MPa when the content of carbon dioxide is 30 percent and 70 percent, and the difference is very large; with the increase of the concentration of the carbon dioxide, the liquefaction pressure of typical 70 percent carbon dioxide is close to that of pure component carbon dioxide, and the liquefaction pressure is respectively 6.5/4.5MPa, the purification system has high purity as much as possible, the liquefaction operation pressure can be greatly reduced, the 6.5MPa type is selected for liquefaction, and the effects of low-temperature refrigeration and high-pressure compression are considered.
TABLE 2 carbon dioxide concentration to operating pressure comparison table
Therefore, the preferred purification system firstly obtains the mixed gas with the carbon dioxide purity of 60-85%, and the mixed gas is liquefied under the conditions of 1-15 ℃ and 3-7.5 MPa, so that good economical efficiency can be obtained;
in the device described above, various changes may be made without departing from the scope of the invention.
Drawings
Fig. 1 is a schematic structural diagram of a purification device for low partial pressure carbon dioxide gas mixture of the present invention.
The symbols in the figure are as follows: 101A and 101B are adsorption towers, B01 is a pressure boosting device, C01 is a pressure boosting device, and PV01 is a product gas buffer tank; PV02 is a waste gas surge tank; TC01 is a refrigerant heat exchanger, and F01 is a filter; YHQ01 is a liquefier, XYQ01 is a silencer, 01A, 02A, 03A, 04A, 01B, 02B, 03B, 04B are automatic control valves, and TV01 is an automatic control valve with flow control regulation capability.
Detailed Description
A typical purification device for carbon dioxide mixed gas with low partial pressure has a structure shown in fig. 1. The method comprises the following steps:
two groups of pressure swing adsorption devices (also called adsorption towers and separators) 101A and 101B are connected in parallel to form two groups of adsorption components which run symmetrically; the two groups of pressure swing adsorption devices are filled with carbon dioxide adsorbents, typically 13X, other modified regenerable carbon dioxide adsorbents with balanced adsorption characteristics;
in addition, water adsorbents (such as one or more of activated alumina, silica gel and other molecular sieves for adsorbing water) are compositely filled at the gas inlet ends of the raw material gases of the two pressure swing adsorption devices so as to remove impurity gases such as water, total hydrocarbons and the like contained in the raw material gas mixture;
the pressure boosting device B01 is used for extracting gas in the adsorption tower and sending the gas into a product gas buffer tank PV 01; the pressure boosting device B01 may be a vacuum pump;
the pressure boosting equipment C01 is used for boosting the pressure of the product carbon dioxide mixed gas to the pressure required by the three phase points of water removal and liquefaction;
a product gas buffer tank PV01 for buffering carbon dioxide product gas;
the exhaust buffer tank PV02 is used for buffering and discharging exhaust gas;
the refrigerant heat exchanger TC01 can be various types of refrigeration equipment and is used for cooling the mixed gas to reduce the water content in the gas;
a filter F01 for removing liquid water droplets contained in the gas phase and discharging the same out of the system;
the liquefier YHQ01 can be various types of refrigeration equipment and heat exchange equipment, is used for cooling gas, meets the requirement of a liquefaction triple point of carbon dioxide mixed gas, and typically adopts a pressure-bearing container (containing heat preservation) for heat exchange by refrigerant water; the liquefier YHQ01 comprises an air inlet, a liquefied carbon dioxide outlet, a non-condensable gas outlet, refrigerant water on-water and a water outlet, and also comprises necessary temperature and pressure monitoring;
the silencer XYQ01 is used for eliminating fluid discharge noise and can be any type of silencer;
still include the control flap: 01A, 02A, 03A, 04A, 01B, 02B, 03B, 04B, and automatic control valves with flow control regulation: TV 01. Wherein:
the raw material gas pipeline is respectively connected with the gas inlets of the adsorption devices 101A and 101B through pipelines, and the control valves 01A and 01B are correspondingly arranged on the two connecting pipelines;
the pressure boosting device B01 is respectively connected with the product air ports of the adsorption devices 101A and 101B through pipelines, and the control valves 02A and 02B are correspondingly arranged on the two connecting pipelines; the other end of the pressure boosting device B01 is connected with the inlet end of a product gas buffer tank PV01 through a pipeline;
the inlet end of the product gas buffer tank PV01 is respectively connected with the product gas ports of the adsorption devices 101A and 101B through pipelines, and the control valves 04A and 04B are correspondingly arranged on the two connecting pipelines;
the inlet end of the exhaust gas buffer tank PV02 is respectively connected with the exhaust gas outlets of the adsorption devices 101A and 101B through pipelines, and the control valves 03A and 03B are correspondingly arranged on the two connecting pipelines; the outlet end of the exhaust buffer tank PV02 is connected with a silencer XYQ01 for discharging the exhaust gas;
the automatic control valve TV01 is arranged on a connecting pipeline of the waste gas outlets of the adsorption devices 101A and 101B;
the inlet end of the refrigerant heat exchanger TC01 is connected with the outlet end of the product gas buffer tank PV01 through a pipeline, and the boosting equipment C01 is arranged on the connecting pipeline; the outlet end of the refrigerant heat exchanger TC01 is sequentially connected with a filter F01 and a liquefier YHQ01 through pipelines.
Generally, the apparatus receives a relatively clean feed gas that has been pretreated, typically after removal of entrained solid particulate impurities and total hydrocarbons such as oil; as is well known in the art, these are very essential to gas separation systems.
The treated raw gas enters a pressure swing adsorption separation device of the prior art described in the attached figure 1, and then carbon dioxide components which are easy to be adsorbed are output from an outlet of a vacuum pump B01, and carbon dioxide with higher purity is output from a product gas buffer tank PV 01.
This pressure swing adsorption device is typical double-tower adsorption system, nitrogen gas in the gas mixture is adsorbed and dispelled to adsorption tower 101A, the difficult gas of adsorbing such as oxygen, adsorption tower 101B is when then accomplishing the regeneration process of adsorbent, the carbon dioxide gas mixture of output enrichment is sent into product gas buffer tank PV01, when adsorption tower 101A adsorbs saturation, switch over promptly and carry out the process of dispelling oxygen, dispelling nitrogen for adsorption tower 101B who has accomplished regeneration, when adsorption tower 101A carries out the regeneration process, the carbon dioxide gas mixture of output enrichment is sent into product gas buffer tank PV01, this kind of pressure swing adsorption process based on balanced adsorption mechanism, heterogeneous order operation when adopting the double-tower device, its typical operation flow is:
(1) opening a control valve TV01, adjusting the opening degree to a certain degree, simultaneously opening control valves 02A and 02B, boosting the pressure of the adsorption tower 101A, and reducing the pressure of the adsorption tower 101B;
(2) opening control valves 01A and 03A, simultaneously introducing the feed gas and the waste gas of the waste gas buffer tank PV102 into an adsorption tower 101A, and pre-pressurizing the adsorption tower 101A; meanwhile, the control valve 02B is opened, and the adsorption tower 101B starts to produce gas and sends the gas into a product gas buffer tank PV 101;
(3) opening a control valve 01A, and allowing feed gas to enter an adsorption tower 101A to continuously perform pre-pressurization; meanwhile, opening a control valve 02B, and generating gas by an adsorption tower 101B;
(4) opening control valves 01A and 03A, feeding and adsorbing the adsorption tower 101A normally, and allowing the gas difficult to adsorb to enter a waste gas buffer tank PV102 and be discharged out of the system; meanwhile, opening a control valve 02B, and generating gas by an adsorption tower 101B;
(5) opening control valves 04A and 03A, and allowing product gas in the buffer tank PV101 to enter 101A to replace the gas phase; meanwhile, opening a control valve 02B, and generating gas by an adsorption tower 101B;
(6) opening a control valve TV01, adjusting the opening degree to a certain degree, simultaneously opening control valves 01A and 03A, and feeding and adsorbing in an adsorption tower 101A; meanwhile, opening a control valve 02B, and generating gas by an adsorption tower 101B;
(7) opening a control valve TV01, adjusting the opening degree to a certain degree, simultaneously opening control valves 02A and 02B, decompressing the adsorption tower 101A, and boosting the pressure of the adsorption tower 101B;
(8) opening a control valve 02A, generating gas by an adsorption tower 101A and sending the gas into a product gas buffer tank PV 101; meanwhile, control valves 01B and 03B are opened, and the feed gas and the waste gas of the waste gas buffer tank PV102 enter the adsorption tower 101B for pre-pressurization;
(9) opening a control valve 02A, and producing gas by an adsorption tower 101A; meanwhile, opening a control valve 01B, and allowing the feed gas to enter an adsorption tower 101B for continuous pre-pressurization;
(10) opening a control valve 02A, and producing gas by an adsorption tower 101A; meanwhile, control valves 01B and 03B are opened, the adsorption tower 101B performs normal adsorption, and the gas difficult to adsorb enters the waste gas buffer tank PV102 and is discharged out of the system;
(11) opening a control valve 02A, and producing gas by an adsorption tower 101A; meanwhile, control valves 04B and 03B are opened, and product gas in the buffer tank PV101 enters 101B to replace the gas phase;
(12) opening a control valve 02A, and producing gas by an adsorption tower 101A; meanwhile, the control valve TV01 is opened and adjusted to a certain opening, and the control valves 01B and 03B are opened to perform feed adsorption, and the adsorption tower 101B performs feed adsorption.
In the above steps, except for the designated open valve, all the other valves are in a closed state, and the opening and flow rate can be controlled by adjusting the TV 01.
In the above steps, after a group of adsorption is saturated, the fluid control valve is controlled and switched to control the fluid to enter the symmetrical adsorption group, and the adsorption group with saturated adsorption is regenerated and gas-produced, and the above steps are repeated in a circulating way, so that the carbon dioxide gas mixture containing oxygen, nitrogen and moisture can be purified to high-purity carbon dioxide with purity of 99% or even more than 99.99%, and the high-purity carbon dioxide gas mixture is continuously sent to a post-stage system.
Furthermore, the utility model discloses, preferably from containing about 15% carbon dioxide gas mixture in typical flue gas, purify and obtain 60 ~ 99.9% carbon dioxide purity, more preferably obtain 60 ~ 85% carbon dioxide purity and send into the back level system in succession.
And, the utility model discloses, the product carbon dioxide gas of extracting in succession through aforementioned step adopts booster compressor C01 pressure boost to 3 ~ 7.5 MPa's pressure to refrigeration through the two-stage coupling is in order to reach the purpose of dispelling moisture and liquefied carbon dioxide respectively, wherein:
preferably, the water in the air is removed by primary refrigeration TC01 under the pressure of 3-7.5 MPa, so as to achieve the process aim of normal pressure dew point of-65 ℃.
The pipe filter F01 is arranged to trap particulates, liquid droplets, which may be present in the pipe and which are discharged from the system via the filter.
Preferably, the process aim of liquefying the mixed gas with the purity of 60-85% of carbon dioxide obtained by the purification system is fulfilled in YHQ01 with a second-stage cold source (second-stage refrigeration, typically, refrigerant water heat exchange) under the conditions of 1-15 ℃ and 3-7.5 MPa, and the non-condensable gas is discharged out of the system.
Therefore, the continuous extraction of the flue gas containing about 15% of carbon dioxide and the purification and liquefaction of the carbon dioxide into liquid carbon dioxide can be completed.
The embodiments described above illustrate only some of the important features of the invention, and all other variations which do not violate the spirit of the invention are also within the scope of the invention, which is limited only by the scope of the claims.
Claims (4)
1. A high purity carbon dioxide gas purification apparatus, comprising:
(1) at least one compression device for providing a pressurized feed gas;
(2) at least one set of pressure swing adsorption device, which at least comprises an adsorption tower, wherein a carbon dioxide adsorbent is filled in the adsorption tower; the system also comprises an air inlet valve for raw material gas to enter each adsorption tower and a necessary connecting pipeline thereof, an exhaust valve for waste gas to enter the waste gas buffer tank and a necessary connecting pipeline thereof, and a gas production valve for product gas to enter the product gas buffer tank and a necessary connecting pipeline thereof; control valves for fluid exchange between symmetrically operating towers and necessary pipelines thereof for regulating and cutting off gas flow between the adsorption towers; the product gas enters the gas inlet valve of each adsorption tower and necessary pipelines thereof;
(3) at least one waste gas buffer tank connected with the exhaust end of each separator through a control valve and a necessary connecting pipeline for receiving waste gas from the separator and sending the temporarily stored waste gas into the separator which is in the process of pre-charging at the exhaust end of the separator;
(4) at least one product gas buffer tank, which is connected with the feed end of each separator through a control valve and a necessary connecting pipeline thereof by a desorption vacuum pump, is used for receiving the product gas from the separator, and sending the product gas in the product buffer tank into the gas inlet end of the separator through the control valve and the necessary connecting pipeline thereof to repressurize the separator which is in the adsorption process;
(5) at least one product gas booster for boosting the product gas in the product gas buffer tank to a predetermined pressure;
(6) at least one refrigerant heat exchanger and a filter, the gas is cooled, the moisture in the gas is condensed into liquid state, and the liquid state is removed through the filter and discharged out of the system;
(7) the at least one heat exchanger is used for cooling the carbon dioxide mixed gas from which the moisture is removed to a liquefaction triple point of the mixed gas, liquefying the carbon dioxide in the mixed gas as a product and outputting the product, and discharging the non-condensable gas out of the system;
(8) and a complete set of control components is used for carrying out necessary operation control on the valves on the loop and carrying out necessary control operation on the compression equipment, the vacuum pump, the refrigeration equipment and the heat exchanger equipment.
2. The apparatus for purifying a high purity carbon dioxide gas as claimed in claim 1, wherein 13X is used as the adsorbent for carbon dioxide.
3. The apparatus for purifying high purity carbon dioxide according to claim 1, wherein a water adsorbent is compositely packed in a gas inlet end of the raw material gas of the pressure swing adsorption apparatus.
4. The apparatus for purifying carbon dioxide gas as claimed in any one of claims 1 to 3, wherein the pressure swing adsorption apparatus, also called adsorption tower or separator, has two sets, denoted 101A, 101B, of adsorption modules connected in parallel, forming two sets of symmetrically operated adsorption modules; the two groups of pressure swing adsorption devices are filled with carbon dioxide adsorbents; further comprising:
the pressure boosting device B01 is used for extracting gas in the adsorption tower and sending the gas into a product gas buffer tank PV 01;
the pressure boosting equipment C01 is used for boosting the pressure of the product carbon dioxide mixed gas to the pressure required by the three phase points of water removal and liquefaction;
a product gas buffer tank PV01 for buffering carbon dioxide product gas;
the exhaust buffer tank PV02 is used for buffering and discharging exhaust gas;
the refrigerant heat exchanger TC01 can be various types of refrigeration equipment and is used for cooling the mixed gas to reduce the water content in the gas;
a filter F01 for removing liquid water droplets contained in the gas phase and discharging the same out of the system;
the liquefier YHQ01 can be various types of refrigeration equipment and heat exchange equipment, is used for cooling gas, meets the three-phase point requirement of liquefaction of carbon dioxide mixed gas, and is typically a pressure-bearing container adopting refrigerant water for heat exchange; the liquefier YHQ01 comprises an air inlet, a liquefied carbon dioxide outlet, a non-condensable gas outlet, refrigerant water on-water and a water outlet, and also comprises necessary temperature and pressure monitoring;
a muffler XYQ01 for canceling fluid discharge noise;
the system also comprises control valves 01A, 02A, 03A, 04A, 01B, 02B, 03B and 04B and an automatic control valve TV01 with flow control and regulation performance; wherein:
the raw material gas pipeline is respectively connected with the gas inlets of the adsorption devices 101A and 101B through pipelines, and the control valves 01A and 01B are correspondingly arranged on the two connecting pipelines;
the pressure boosting device B01 is respectively connected with the product air ports of the adsorption devices 101A and 101B through pipelines, and the control valves 02A and 02B are correspondingly arranged on the two connecting pipelines; the other end of the pressure boosting device B01 is connected with the inlet end of a product gas buffer tank PV01 through a pipeline;
the inlet end of the product gas buffer tank PV01 is respectively connected with the product gas ports of the adsorption devices 101A and 101B through pipelines, and the control valves 04A and 04B are correspondingly arranged on the two connecting pipelines;
the inlet end of the exhaust gas buffer tank PV02 is respectively connected with the exhaust gas outlets of the adsorption devices 101A and 101B through pipelines, and the control valves 03A and 03B are correspondingly arranged on the two connecting pipelines; the outlet end of the exhaust buffer tank PV02 is connected with a silencer XYQ01 for discharging the exhaust gas;
the automatic control valve TV01 is arranged on a connecting pipeline of the waste gas outlets of the adsorption devices 101A and 101B;
the inlet end of the refrigerant heat exchanger TC01 is connected with the outlet end of the product gas buffer tank PV01 through a pipeline, and the boosting equipment C01 is arranged on the connecting pipeline; the outlet end of the refrigerant heat exchanger TC01 is sequentially connected with a filter F01 and a liquefier YHQ01 through pipelines.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
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| WO2023066105A1 (en) * | 2021-10-19 | 2023-04-27 | 大连理工大学 | System and method for synchronously recovering nitrogen and carbon dioxide from boiler flue gas |
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