Carbon dioxide purification system

Abstract

The present disclosure relates to the field of carbon dioxide refining. The carbon dioxide refining system of the present disclosure includes an oxygen conveying device, a carbon dioxide conveying device, a reaction device, a first heater, a heat exchange device and a distillation device. The oxygen conveying device has an oxygen output port. The carbon dioxide conveying device has a carbon dioxide output port. The reaction device has a reaction inlet and a reaction outlet. The first heater is used to heat the mixed oxygen and carbon dioxide. The heat exchange device has a first heat exchange channel and a second heat exchange channel that can exchange heat. The inlet of the first heat exchange channel is connected to the carbon dioxide output port, and the outlet is interconnected with the oxygen output port and connected to the reaction inlet, and the inlet of the second heat exchange channel is connected to the reaction outlet. The distillation device is connected to the outlet of the second heat exchange channel, and is used for distilling and removing light component impurities and heavy component impurities in the heat-exchanged reaction material. The carbon dioxide refining system of the present disclosure consumes little energy during operation.

Description

Technical Field

[0001] The present disclosure relates to the technical field of carbon dioxide refining, and in particular to a refining system for electronic grade carbon dioxide. Background Art

[0002] In the related art, the production method of electronic-grade carbon dioxide includes refining food-grade liquid carbon dioxide as a raw material to obtain electronic-grade liquid carbon dioxide with higher purity.

[0003] Food-grade liquid carbon dioxide contains water (H2O), alkanes (C m H n ), carbonyl sulfide (COS), oxygen (O2) and nitrogen (N2) and other impurities. When refining equipment is used to refine food-grade liquid carbon dioxide, the liquid carbon dioxide is first purified by a gasification device, and then the impurities in the gaseous carbon dioxide are removed by a distillation device. When the system is running, additional heat from the gasification device is required to gasify the liquid carbon dioxide, which consumes a lot of energy.

[0004] In addition, distillation devices often use refrigerant heat exchange to remove impurities in gaseous carbon dioxide. When the distillation equipment is running, the pressure in the pipeline is high, the energy consumption is high, and the amount of refrigerant used is large, resulting in high operating costs for the equipment. Summary of the invention

[0005] In view of the above-mentioned shortcomings of the prior art, an object of the present disclosure is to provide a carbon dioxide refining system which consumes little energy during operation.

[0006] The carbon dioxide refining system provided by the present disclosure includes: an oxygen conveying device having an oxygen output port for outputting oxygen; a carbon dioxide conveying device having a carbon dioxide output port for outputting liquid carbon dioxide; a reaction device having a reaction inlet and a reaction outlet for reacting oxygen with impurities in carbon dioxide to form a reacted material; a first heater, arranged in the reaction device or in the front stage of the reaction device, for heating the mixed oxygen and carbon dioxide; a heat exchange device having a first heat exchange channel and a second heat exchange channel capable of heat exchange, the inlet of the first heat exchange channel being connected to the carbon dioxide output port, the outlet being interconnected with the oxygen output port and connected to the reaction inlet, and the inlet of the second heat exchange channel being connected to the reaction outlet; and a rectification device, connected to the outlet of the second heat exchange channel, for rectifying and removing light component impurities and heavy component impurities in the reacted material after heat exchange.

[0007] According to some embodiments provided by the present disclosure, the distillation device includes: a first rectifier, having a first feed port, which is connected to the outlet of the second heat exchange channel; a first reboiler, which is arranged corresponding to the bottom of the first rectifier and has a first reboiler inlet and a first reboiler outlet for coolant to flow in and out, respectively, for circulating the refrigerant and exchanging heat with the liquid at the bottom of the first rectifier; a first condenser, which is arranged corresponding to the top of the first rectifier and has a first condensation inlet and a first condensation outlet, which is connected to the first reboiler outlet, for circulating the refrigerant and exchanging heat with the gas at the top of the first condenser; and a first compressor, whose inlet is connected to the first condensation outlet and whose outlet is connected to the first reboiler inlet.

[0008] According to some embodiments provided in the present disclosure, a third heat exchange channel capable of exchanging heat with the second heat exchange channel is provided in the heat exchange device, and an inlet of the third heat exchange channel is connected to an outlet of the first rectifier for outputting heavy component impurities.

[0009] According to some embodiments provided by the present disclosure, a fourth heat exchange channel capable of exchanging heat with the second heat exchange channel is provided in the heat exchange device, and the inlet of the fourth heat exchange channel is connected to the outlet of the first condenser for outputting condensed light component impurities.

[0010] According to some embodiments provided by the present disclosure, the distillation device includes: a second rectifier, having a second feed port, the second feed port is connected to the first discharge port at the top of the first rectifier; a second reboiler, arranged corresponding to the bottom of the second rectifier, and having a second reboiler inlet and a second reboiler outlet, the second reboiler inlet is connected to the outlet of the first compressor; a second condenser, having a first cold inlet, a first cold outlet, a second cold inlet and a second cold outlet, the first cold inlet is connected to the second reboiler outlet, the first cold outlet is connected to the inlet of the first compressor, and the second cold inlet and the second cold outlet are respectively connected to the outlet and inlet of the top of the second rectifier; a fourth heat exchange channel capable of exchanging heat with the second heat exchange channel is provided in the heat exchange device, and the inlet of the fourth heat exchange channel is connected to the second cold outlet.

[0011] According to some embodiments provided by the present disclosure, the distillation device also includes: a subcooler, having a first subcooling inlet, a first subcooling outlet, a second subcooling inlet and a second subcooling outlet, the first subcooling inlet is connected to the second reboiler outlet, the first subcooling outlet is connected to the inlet of the first compressor, the second subcooling inlet is connected to the second heavy component outlet at the bottom of the second rectifier, and the second subcooling outlet is connected to a second storage container.

[0012] According to some embodiments provided by the present disclosure, it also includes: a heat exchange device, having a first heat exchange inlet, a first heat exchange outlet, a second heat exchange inlet and a second heat exchange outlet, the first heat exchange inlet is connected to the oxygen output port and the outlet of the first heat exchange channel, the second heat exchange inlet is connected to the reaction outlet, and the second heat exchange outlet is connected to the inlet of the second heat exchange channel; a desulfurization device, having a desulfurization inlet and a desulfurization outlet, the desulfurization inlet is connected to the first heat exchange outlet, and the desulfurization outlet is connected to the reaction inlet.

[0013] According to some embodiments provided by the present disclosure, the system further includes: a second compressor, whose inlet is connected to the reaction outlet, and whose outlet is connected to the second heat exchange inlet.

[0014] According to some embodiments provided by the present disclosure, it also includes: a cooling device connected to the rear stage of the reaction device; an adsorption device, which provides a built-in adsorbent capable of absorbing water and is connected to the rear stage of the cooling device and the front stage of the second heat exchange channel.

[0015] According to some embodiments provided by the present disclosure, the adsorption device includes: a first adsorber; a second adsorber, which is arranged in parallel with the first adsorber; a regeneration gas input pipeline and a second heater, the second heater being used to heat the regeneration gas transported by the regeneration gas input pipeline; and when one of the first adsorber and the second adsorber is connected to the reaction outlet and the inlet of the second heat exchange channel, the regeneration gas input pipeline is connected to the other of the first adsorber and the second adsorber.

[0016] Beneficial Effects

[0017] (1) The carbon dioxide purification system disclosed in the present invention does not require the introduction of additional heat from the gasification device and consumes little energy during operation.

[0018] (2) In the carbon dioxide refining system disclosed in the present invention, the liquid carbon dioxide as a raw material can cool the gaseous carbon dioxide to be introduced into the distillation device, so that the pressure required for the refrigerant during distillation is small, the energy consumption for compressing the refrigerant is small, and the amount of refrigerant used is small.

[0019] (3) In the carbon dioxide refining system disclosed in the present invention, the heavy component impurities produced after distillation can increase the liquid phase material content in the reacted material to be introduced into the distillation device, so that the pressure required for the refrigerant during distillation is small, the energy consumption for compressing the refrigerant is small, and the amount of refrigerant used is small.

[0020] (4) In the carbon dioxide refining system disclosed in the present invention, the light component impurities generated after distillation can increase the liquid phase material content in the reacted material to be introduced into the distillation device, so that the pressure required for the refrigerant during distillation is small, the energy consumption for compressing the refrigerant is small, and the amount of refrigerant used is small.

[0021] (5) In the carbon dioxide refining system disclosed in the present invention, the heat exchange device is helpful to reduce the heating burden in the carbon dioxide impurity removal process and improve the desulfurization effect of carbon dioxide. BRIEF DESCRIPTION OF THE DRAWINGS

[0022] Figure 1 It is a schematic diagram of the layout of the carbon dioxide refining system according to an embodiment of the present disclosure.

[0023] Figure 2 It is a schematic diagram of the enlarged layout of the distillation device and the heat exchange device of the embodiment of the present disclosure.

[0024] Figure 3 A schematic diagram of the adsorption device disclosed in the present invention in a first working state.

[0025] Figure 4 A schematic diagram of the adsorption device of the present invention in the second working state.

[0026] Figure 5 A schematic diagram of the adsorption device disclosed in the present invention in the third working state.

[0027] Figure 6 Schematic diagram of the adsorption device of the present invention in the fourth working state.

[0028] Reference numerals:

[0029] Oxygen delivery device 11; oxygen outlet 1101; oxygen delivery pipeline 111; oxygen storage container 112;

[0030] Carbon dioxide delivery device 12; carbon dioxide output port 1201; carbon dioxide delivery pipeline 121; first storage container 122;

[0031] Reaction device 13; reaction inlet 1301; reaction outlet 1302;

[0032] A first heater 14;

[0033] Heat exchange device 15; first heat exchange channel 1501; second heat exchange channel 1502; third heat exchange channel 1503; fourth heat exchange channel 1504;

[0034] Heat exchange device 16; first heat exchange inlet 1601; first heat exchange outlet 1602; second heat exchange inlet 1603; second heat exchange outlet 1604;

[0035] Desulfurization device 17; desulfurization inlet 1701; desulfurization outlet 1702;

[0036] A second compressor 18;

[0037] Cooling device 19;

[0038] Adsorption device 21; first adsorber 211; second adsorber 212; regeneration gas input pipeline 213; second heater 214; regeneration gas output pipeline 215; venting pipeline 216; first valve a; second valve b; third valve c; fourth valve d; fifth valve e; sixth valve f; seventh valve g; eighth valve h; ninth valve i; tenth valve j;

[0039] Heat recovery device 22; first heat recovery inlet 2201; first heat recovery outlet 2202; second heat recovery inlet 2203; second heat recovery outlet 2204;

[0040] Rectification device 800; first rectifier 81; first feed inlet 8101; first heavy component outlet 8102; first discharge port 8103; first reboiler 82; first reboiler inlet 8201; first reboiler outlet 8202; first condenser 83; first condensation inlet 8301; first condensation outlet 8302; second condensation inlet 8303; second condensation outlet 8304; first compressor 84; first throttle valve 85; second rectifier 86; second feed inlet 8601; second reboiler Branch outlet 8602; second reboiler 87; second reboiler inlet 8701; second reboiler outlet 8702; second condenser 88; first cold inlet 8801; first cold outlet 8802; second cold inlet 8803; second cold outlet 8804; second throttle valve 89; subcooler 91; first subcooling inlet 9101; first subcooling outlet 9102; second subcooling inlet 9103; second subcooling outlet 9104; second storage container 92; third throttle valve 93; fourth throttle valve 94. DETAILED DESCRIPTION

[0041] The following is an explanation of the embodiments of the present disclosure by specific examples, and those skilled in the art can easily understand other advantages and effects of the present disclosure from the information disclosed by the present disclosure. The present disclosure can also be implemented or applied through other different specific embodiments, and the details in the present disclosure can also be modified or changed in various ways according to different viewpoints and application modules without departing from the spirit of the present disclosure. It should be noted that the embodiments in the present disclosure and the features in the embodiments can be combined with each other without conflict.

[0042] The following is a detailed description of the embodiments of the present disclosure with reference to the accompanying drawings so that those skilled in the art can easily implement the present disclosure. The present disclosure can be embodied in many different forms and is not limited to the embodiments described herein.

[0043] In the representations of the present disclosure, the reference terms "one embodiment", "some embodiments", "examples", "specific examples", or "some examples" and the like mean that the specific features, structures, materials or characteristics represented in conjunction with the embodiment or example are included in at least one embodiment or example of the present disclosure. Moreover, the specific features, structures, materials or characteristics represented may be combined in any one or a group of embodiments or examples in a suitable manner. In addition, those skilled in the art may combine and combine different embodiments or examples represented in the present disclosure and the features of different embodiments or examples, unless they are mutually contradictory.

[0044] In addition, the terms "first" and "second" are used for descriptive purposes only and should not be understood as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Therefore, a feature defined as "first" or "second" may explicitly or implicitly include at least one of the features. In the representation of the present disclosure, "a group" means two or more, unless otherwise clearly and specifically defined.

[0045] In order to clearly describe the present disclosure, components not related to the description are omitted, and the same reference numerals are given to the same or similar components throughout the specification.

[0046] Throughout the specification, when a device is said to be "connected" to another device, this includes not only the case of "direct connection" but also the case of "indirect connection" by placing other elements therebetween. In addition, when a device is said to "include" a certain component, unless otherwise stated, it does not exclude other components, but means that other components may be included.

[0047] Although the terms first, second, etc. are used to represent various elements in this article in some examples, these elements should not be limited by these terms. These terms are only used to distinguish one element from another element. For example, the first interface and the second interface, etc. are represented. Moreover, as used in this article, the singular forms "one", "one" and "the" are intended to also include plural forms, unless there is an opposite indication in the context. It should be further understood that the terms "comprising" and "including" indicate that there are the described features, steps, operations, elements, modules, projects, kinds, and / or groups, but do not exclude the existence, occurrence or addition of one or a group of other features, steps, operations, elements, modules, projects, kinds, and / or groups. The terms "or" and "and / or" used herein are interpreted as inclusive, or mean any one or any combination. Therefore, "A, B or C" or "A, B and / or C" means "any of the following: A; B; C; A and B; A and C; B and C; A, B and C". Only when the combination of elements, functions, steps or operations is inherently mutually exclusive in some way, will there be an exception to this definition.

[0048] The technical terms used herein are only used to refer to specific embodiments and are not intended to limit the present disclosure. The singular form used herein also includes the plural form unless the sentence clearly indicates the contrary meaning. The meaning of "including" used in the specification is to specify specific characteristics, regions, integers, steps, operations, elements and / or components, and does not exclude the existence or addition of other characteristics, regions, integers, steps, operations, elements and / or components.

[0049] Although not defined differently, all terms, including technical and scientific terms used herein, have the same meaning as those generally understood by those skilled in the art to which the present disclosure belongs. Terms defined in commonly used dictionaries are additionally interpreted as having meanings consistent with relevant technical literature and the message of the present disclosure, and shall not be overly interpreted as ideal or very formal meanings unless defined.

[0050] In the related art, during the process of refining carbon dioxide, the liquid carbon dioxide is first gasified by a gasification device, and then the impurities in the gaseous carbon dioxide are removed by a distillation device. When the system is running, additional heat from the gasification device is required to gasify the liquid carbon dioxide, which consumes a lot of energy.

[0051] In view of this, the present disclosure provides a carbon dioxide refining system, which consumes little energy when in operation.

[0052] Figure 1 Schematic diagram of the layout of the carbon dioxide refining system according to the embodiment of the present disclosure. Figure 1 The carbon dioxide refining system of the embodiment of the present disclosure includes an oxygen delivery device 11, a carbon dioxide delivery device 12, a reaction device 13, a first heater 14, a heat exchange device 15 and a distillation device 800.

[0053] The oxygen delivery device 11 has an oxygen output port 1101 for outputting gaseous oxygen. Optionally, the oxygen delivery device 11 includes an oxygen delivery pipeline 111. The oxygen delivery pipeline 111 is provided with the oxygen output port 1101 for outputting gaseous oxygen. The oxygen delivery device 11 also includes an oxygen storage container 112. The oxygen storage container 112 is connected to the oxygen delivery pipeline 111 to provide gaseous oxygen to the oxygen delivery pipeline 111.

[0054] The carbon dioxide delivery device 12 has a carbon dioxide output port 1201 for outputting liquid carbon dioxide. Optionally, the carbon dioxide delivery device 12 includes a carbon dioxide delivery pipeline 121. The carbon dioxide delivery pipeline 121 is provided with the carbon dioxide output port 1201 to output liquid carbon dioxide. Optionally, the carbon dioxide delivery device 12 also includes a first storage container 122. The first storage container 122 is in communication with the carbon dioxide delivery pipeline 121 to provide liquid carbon dioxide to the carbon dioxide delivery pipeline 121.

[0055] The reaction device 13 has a reaction inlet 1301 and a reaction outlet 1302, which are used to supply oxygen and impurities in carbon dioxide to react, thereby achieving the effect of removing impurities (such as alkane impurities). Specifically, the following reactions mainly occur in the reaction device 13: C m H n +(m+n / 4)O2=mCO2+n / 2H2O.

[0056] The first heater 14 is provided in the reaction device 13 or in the front stage of the reaction device 13, and is used to heat the mixed oxygen and carbon dioxide, thereby providing heat for the reaction of oxygen and impurities in the reaction device 13. Optionally, the first heater 14 is an electric heater, which is easy to operate, pollution-free, and convenient to adjust the heating power.

[0057] The heat exchange device 15 has a first heat exchange channel 1501 and a second heat exchange channel 1502. The inlet of the first heat exchange channel 1501 is connected to the carbon dioxide output port 1201, and the outlet is interconnected with the oxygen output port 1101 and connected to the reaction inlet 1301. The inlet of the second heat exchange channel 1502 is connected to the reaction outlet 1302. The distillation device 800 is connected to the outlet of the second heat exchange channel 1502, and is used to distill and remove light component impurities and heavy component impurities in the heat exchanged reaction material.

[0058] Understandably, Figure 1 The arrows shown on the solid line and the arrows at the first heat exchange channel 1501 and the second heat exchange channel 1502 indicate the flow direction of carbon dioxide when the system is running.

[0059] Therefore, before the liquid carbon dioxide output from the carbon dioxide delivery device 12 is mixed with the gaseous oxygen output from the oxygen delivery device 11, the liquid carbon dioxide can exchange heat with the post-reaction material output from the reaction device 13, so that the heat brought by the heating in the process of removing impurities can be used to heat the liquid carbon dioxide to gasify and then be delivered to the reaction device 13, and the post-reaction material after heat exchange is then delivered to the distillation device 800, without the need to additionally use the heat brought by the gasification device, and the energy consumption is small.

[0060] Optionally, the distillation device 800 includes a first rectifier 81 , a first reboiler 82 , a first condenser 83 and a first compressor 84 .

[0061] Figure 2 It is a schematic diagram of the enlarged layout of the distillation device and the heat exchange device of the embodiment of the present disclosure. Figure 1 and Figure 2 The arrows shown on the dotted lines except for the heat exchange device 15 indicate the flow direction of the refrigerant when the rectification device 800 is in operation. Figure 1 and Figure 2 The first rectifier 81 (for example, the first distillation tower) has a first feed port 8101, and the first feed port 8101 is connected to the outlet of the second heat exchange channel 1502. Therefore, the post-reaction material after heat exchange can be transported to the first rectifier 81 through the first feed port 8101. Since the post-reaction material absorbs the coldness of the liquid phase carbon dioxide to cool down during the heat exchange process, the post-reaction material after heat exchange carries more liquid phase material, and the post-reaction material carrying more liquid phase material can enter the first rectifier 81 through the first feed port 8101.

[0062] The first reboiler 82 is arranged corresponding to the bottom of the first rectifier 81, and has a first reboiler inlet 8201 and a first reboiler outlet 8202 for respectively allowing the refrigerant to flow in and out, and is used for the refrigerant to circulate and exchange heat with the liquid at the bottom of the first rectifier 81.

[0063] Optionally, the first reboiler 82 is arranged inside the bottom of the first rectifier 81. Therefore, in the process of the refrigerant flowing from the first reboiler inlet 8201 to the first reboiler outlet 8202, it can exchange heat with the liquid phase material at the bottom of the first rectifier 81, so that the refrigerant absorbs cold energy and cools down, and the light components (components containing more oxygen and nitrogen) in the liquid phase material absorb heat and become gas phase and rise to the top of the first rectifier 81, and the heavy components (components containing more alkane impurities) in the liquid phase material are retained and gathered at the bottom of the first rectifier 81. Of course, it can be understood that the setting position of the first reboiler 82 includes but is not limited to this, and the first reboiler 82 can also be arranged outside the bottom of the first rectifier 81.

[0064] The first condenser 83 is arranged corresponding to the top of the first rectifier 81, and has a first condensation inlet 8301 and a first condensation outlet 8302. The first condensation inlet 8301 is connected to the first reboiler outlet 8202, and is used for the circulation of the reboiled refrigerant and heat exchange with the gas at the top of the first rectifier 81. Therefore, the refrigerant after absorbing cold and cooling in the first reboiler 82 can be passed into the first condensation inlet 8301, and flow to the first condensation outlet 8302 through the first condensation inlet 8301. In this process, the refrigerant can exchange heat with the gas phase carbon dioxide at the top of the first rectifier 81, so that most of the gas phase material is condensed into a liquid phase material containing a small amount of oxygen and nitrogen. The liquid phase material flows back from the top of the first rectifier 81 to the bottom of the first rectifier 81, and the reboiler-condenser cycle continues. At the same time, the gas phase material containing a large amount of oxygen and nitrogen that has not been condensed is retained and accumulated at the top.

[0065] The inlet of the first compressor 84 (eg, the first compressor) is connected to the first condensation outlet 8302, and the outlet is connected to the first reboiler inlet 8201, which is used to pressurize the refrigerant, increase the temperature and pressure of the refrigerant and transport it to the first reboiler 82, so that the refrigerant can circulate smoothly.

[0066] Specifically, when the first rectifier 81 of the present disclosure rectifies and processes the post-reaction material containing more liquid phase material, i.e., liquid, the distillation process is specifically as follows:

[0067] After the reacted material containing more liquid phase material is input into the first distillation vessel 81, the liquid phase material directly flows to the bottom of the first distillation vessel 81 and absorbs the heat carried by the refrigerant circulating in the first reboiler 82, so that the light components (components containing more oxygen and nitrogen) in the liquid phase material are transformed into gas phase and rise to the top of the first distillation vessel 81, and the heavy components (components containing more alkane impurities) in the liquid phase material remain at the bottom of the first distillation vessel 81, so that the heavy component impurities (alkane impurities) can be gradually accumulated at the bottom of the first distillation vessel 81, thereby gradually separating the heavy component impurities.

[0068] The gaseous material flows directly to the top of the first distillation vessel 81 and absorbs the cold energy carried by the refrigerant circulating in the first condenser 83, so that the gaseous material can be condensed into a liquid phase and fall toward the bottom of the first distillation vessel 81, thereby continuing the reboiling-condensing cycle, and the uncondensed light components of the gaseous material (components containing more oxygen and nitrogen) remain at the top of the first distillation vessel 81, thereby gradually gathering light component impurities (oxygen and nitrogen impurities) at the top of the first distillation vessel 81, thereby gradually separating the light component impurities. In the above process, since the carbon dioxide contains more liquid-phase materials when it is introduced into the first distillation vessel 81, more liquid-phase materials directly flow to the first reboiler 82 and are separated from heavy impurities by the first reboiler 82. Therefore, the separation effect of the heavy impurities (alkane impurities) in the carbon dioxide is good and the separation speed is fast, and it is beneficial to reduce the reflux amount of carbon dioxide during the circulation of the distillation process, and it is beneficial to reduce the refrigerant flow required in the distillation process and the compression burden of the first compressor 84. For example, the first compressor 84 compresses the refrigerant to a relatively low pressure (for example, compressed to a gas-phase refrigerant with a pressure of 0.3 MPa) and then outputs it. Therefore, when the distillation device of the present disclosure is in operation, the compression pressure required by the first compressor 84 is low, the energy consumption is small, and the amount of refrigerant used is small.

[0069] Optionally, see Figure 1 and Figure 2 The heat exchange device 15 is provided with a third heat exchange channel 1503 capable of exchanging heat with the second heat exchange channel 1502. The inlet of the third heat exchange channel 1503 is connected to the outlet of the first rectifier 81 for outputting heavy component impurities. The arrow at the third heat exchange channel 1503 indicates the flow direction of the heavy component impurities in the carbon dioxide after rectification. For example, the first heavy component outlet 8102 is provided at the bottom of the first rectifier 81, and the inlet of the third heat exchange channel 1503 is connected to the first heavy component outlet 8102.

[0070] Therefore, when the heavy component impurities output from the first heavy component outlet 8102 flow through the third heat exchange channel 1503, they can exchange heat with the reacted material flowing through the second heat exchange channel 1502, so that the reacted material further absorbs cold energy to be cooled and liquefied and then input into the first rectifier 81, so as to further reduce the compression pressure and the amount of refrigerant required by the first compressor 84. At the same time, the heavy component impurities absorb heat and heat up to room temperature, so that they can be conveniently discharged from the outlet of the third heat exchange channel 1503.

[0071] Optionally, see Figure 1 and Figure 2The heat exchange device 15 is provided with a fourth heat exchange channel 1504 capable of exchanging heat with the second heat exchange channel 1502. The inlet of the fourth heat exchange channel 1504 is connected to the outlet of the first condenser 83 for outputting the condensed light component impurities. The arrow at the fourth heat exchange channel 1504 indicates the flow direction of the light component impurities in the carbon dioxide after distillation. For example, the first condenser 83 has a second condensation inlet 8303 and a second condensation outlet 8304 respectively connected to the outlet and inlet of the top of the first rectifier 81, and the inlet of the fourth heat exchange channel 1504 is connected to the second condensation outlet 8304. Specifically, the inlet of the fourth heat exchange channel 1504 is connected to the connecting pipeline between the top of the first rectifier 81 and the second condensation outlet 8304. Thus, the gaseous material can flow into the first condenser 83 from the second condensation inlet 8303, and exchange heat with the refrigerant in the process of flowing to the second condensation outlet 8304, thereby condensing into a liquid phase and then reflux to the top of the first rectifier 81 through the second condensation outlet 8304, and the condensed light component impurities output from the second condensation outlet 8304 can be output to the fourth heat exchange channel 1504.

[0072] Therefore, when the condensed light component impurities output from the second condensation outlet 8304 flow through the fourth heat exchange channel 1504, they can exchange heat with the post-reaction material flowing through the second heat exchange channel 1502, so that the post-reaction material further absorbs cold energy to cool down and liquefy and then input into the first distillation device 81, so as to further reduce the compression pressure and the amount of refrigerant required by the first compressor 84. At the same time, the condensed light component impurities absorb heat and heat up to room temperature, so that they can be conveniently discharged from the outlet of the fourth heat exchange channel 1504.

[0073] More preferably, the heat exchange device 15 of the present disclosure has both the third heat exchange channel 1503 and the fourth heat exchange channel 1504, so that the total cooling capacity provided by the first heat exchange channel 1501, the third heat exchange channel 1503, the fourth heat exchange channel 1504 and other multiple heat exchange channels can better cool and liquefy the reacted material, so that the reacted material to be input into the first rectifier 81 can carry a large amount of liquid, thereby further reducing the compression pressure and the amount of refrigerant required by the first compressor 84. Of course, it can be understood that Figure 1 and Figure 2 The first heat exchange channel 1501, the second heat exchange channel 1502, the third heat exchange channel 1503 and the fourth heat exchange channel 1504 shown in the figure are only simple illustrations for the convenience of understanding of those skilled in the art, and are not the specific structures of each heat exchange channel. The heat exchange device 15 of the example disclosed in the present invention is a multi-stream heat exchanger capable of heat exchange for multiple streams, and can be a plate-fin heat exchanger.

[0074] Optionally, see Figure 2 The rectification device 800 further includes a first throttle valve 85. The first throttle valve 85 is provided in the connecting pipeline between the first reboiler outlet 8202 and the first condenser inlet 8301. Thus, after the refrigerant is output from the first reboiler outlet 8202, it will be throttled and depressurized by the first throttle valve 85 to further reduce the temperature before being transported to the first condenser inlet 8301, thereby improving the condensation effect.

[0075] Optionally, the distillation device 800 further includes a second distillation vessel 86, a second reboiler 87, and a second condenser 88. The second distillation vessel 86 (e.g., a second distillation tower) has a second feed port 8601, and the second feed port 8601 is connected to a first discharge port 8103 at the top of the first distillation vessel 81. Thus, during the operation of the distillation device 800, a liquid phase material containing a small amount of oxygen and nitrogen from the top of the first distillation vessel 81 can enter the first distillation vessel 81 through the second feed port 8601.

[0076] The second reboiler 87 is arranged corresponding to the bottom of the second rectifier 86, and has a second reboiler inlet 8701 and a second reboiler outlet 8702 for respectively allowing the refrigerant to flow in and out, and is used for the refrigerant to circulate and exchange heat with the liquid at the bottom of the second rectifier 86.

[0077] Optionally, the second reboiler 87 is arranged inside the bottom of the second rectifier 86. Thus, in the process of the refrigerant flowing from the second reboiler inlet 8701 to the second reboiler outlet 8702, it can exchange heat with the liquid phase material located at the bottom of the second rectifier 86, so that the refrigerant absorbs cold energy and cools down, and the light components (components containing more oxygen and nitrogen) in the liquid phase material absorb heat and become gas phase and rise to the top of the second rectifier 86, and the liquid carbon dioxide is retained and gathered at the bottom of the first rectifier 81, thereby gradually separating the liquid carbon dioxide with higher purity. Of course, it can be understood that the setting position of the second reboiler 87 includes but is not limited to this, and the second reboiler 87 can also be arranged outside the bottom of the second rectifier 86.

[0078] The second condenser 88 is arranged corresponding to the top of the second rectifier 86, and has a first cold inlet 8801 and a first cold outlet 8802. The first cold inlet 8801 is connected to the second reboiler outlet 8702, and is used for the reboiled refrigerant to circulate and exchange heat with the gas at the top of the second rectifier 86. Therefore, the refrigerant after absorbing cold energy and cooling in the second reboiler 87 can pass into the first cold inlet 8801, and flow to the first cold outlet 8802 through the first cold inlet 8801. Thereafter, the refrigerant can exchange heat with the gaseous material at the top of the second distillation vessel 86, so that most of the gaseous material is condensed into a liquid material containing a smaller amount of oxygen and nitrogen. The liquid material flows back from the top of the second distillation vessel 86 to the bottom of the second distillation vessel 86, and the reboiling-condensing cycle is continued. The uncondensed light components of the gaseous material (components containing more oxygen and nitrogen) remain at the top of the second distillation vessel 86, so that the light component impurities (oxygen and nitrogen impurities) can be gradually accumulated at the top of the second distillation vessel 86, thereby further separating the light component impurities.

[0079] The inlet of the first compressor 84 (eg, the first compressor) is connected to the first cold outlet 8802, and the outlet is connected to the second reboiler inlet 8701, for pressurizing the refrigerant, increasing the temperature and pressure of the refrigerant and delivering it to the second reboiler 87, so that the refrigerant can circulate smoothly.

[0080] Optionally, the second condenser 88 has a second cold inlet 8803 and a second cold outlet 8804 which are respectively connected to the outlet and the inlet of the top of the second rectifier 86. Thus, the gaseous material can flow into the second condenser 88 from the second cold inlet 8803, and exchange heat with the refrigerant in the process of flowing to the second cold outlet 8804, so as to be condensed into a liquid phase and then flow back to the top of the second rectifier 86. The inlet of the fourth heat exchange channel 1504 is connected to the connecting pipeline between the top of the second rectifier 86 and the second cold outlet 8804. Thus, the condensed light component impurities output by the second condenser 88 can be output to the fourth heat exchange channel 1504. In this way, when the condensed light component impurities output by the second rectifier 86 flow through the fourth heat exchange channel 1504, they can exchange heat with the reacted material flowing through the second heat exchange channel 1502, so that the reacted material further absorbs cold to cool and liquefy, and the liquid phase material content in the reacted material is further increased.

[0081] More preferably, both the first rectifier 81 and the second rectifier 86 can output the condensed light component impurities to the fourth heat exchange channel 1504. Therefore, the flow rate of the condensed light component impurities flowing through the fourth heat exchange channel 1504 is large, which can provide more cooling capacity for the reacted material to be input into the first rectifier 81, which is conducive to further increasing the content of liquid phase material in the reacted material.

[0082] Optionally, the rectification device 800 further includes a second throttle valve 89. The second throttle valve 89 is disposed in a connecting pipeline between the second reboiler outlet 8702 and the first cold inlet 8801. Thus, after the refrigerant is output from the second reboiler outlet 8702, it is throttled and depressurized by the second throttle valve 89 to further reduce the temperature before being transported to the first cold inlet 8801, so as to improve the condensation effect of the second condenser 88.

[0083] Optionally, the distillation device 800 further includes a subcooler 91. The subcooler 91 has a first subcooling inlet 9101, a first subcooling outlet 9102, a second subcooling inlet 9103 and a second subcooling outlet 9104. The first subcooling inlet 9101 is connected to the second reboiler outlet 8702. The first subcooling outlet 9102 is connected to the inlet of the first compressor 84. The second subcooling inlet 9103 is connected to the second heavy component outlet 8602 at the bottom of the second rectifier 86, and the second subcooling outlet 9104 is connected to the second storage container 92. Thus, in the subcooler 91, the refrigerant can exchange heat with the liquid carbon dioxide output from the second rectifier 86, so that the refrigerant absorbs heat to increase the temperature, and the carbon dioxide absorbs cold to further reduce the temperature, thereby ensuring that the output carbon dioxide can be fully cooled and liquefied, and then stored in the second storage container 92 in the liquid phase.

[0084] Optionally, the rectification device 800 further includes a third throttle valve 93. The third throttle valve 93 is disposed in a connecting pipeline between the second reboiler outlet 8702 and the first subcooling inlet 9101. Thus, after the refrigerant is output from the second reboiler outlet 8702, it is throttled and depressurized by the third throttle valve 93 to further reduce the temperature before being transported to the first subcooling inlet 9101, so as to improve the subcooling effect of the subcooler 91.

[0085] Optionally, see Figure 2, the rectification device 800 further includes a fourth throttle valve 94. The fourth throttle valve 94 is provided in the connecting pipeline between the first outlet 8103 and the second feed port 8601. Thus, after the refrigerant is output from the first outlet 8103, it will be throttled and depressurized by the fourth throttle valve 94 to further reduce the temperature before being transported to the second feed port 8601, which is conducive to ensuring that the carbon dioxide enters the second feed port 8601 in the liquid phase.

[0086] Optionally, see Figure 1 The carbon dioxide refining system also includes a heat exchange device 16 and a desulfurization device 17.

[0087] The heat exchange device 16 has a first heat exchange inlet 1601, a first heat exchange outlet 1602, a second heat exchange inlet 1603 and a second heat exchange outlet 1604. The first heat exchange inlet 1601 is connected to the oxygen output port 1101 and the outlet of the first heat exchange channel 1501. The second heat exchange inlet 1603 is connected to the reaction outlet 1302, and the second heat exchange outlet 1604 is connected to the inlet of the second heat exchange channel 1502. The desulfurization device 17 is provided with a built-in desulfurizer, and the desulfurization device 17 has a desulfurization inlet 1701 and a desulfurization outlet 1702. And the desulfurization inlet 1701 is connected to the first heat exchange outlet 1602. The desulfurization outlet 1702 is connected to the reaction inlet 1301. For example, the heat exchange device can be a shell and tube heat exchanger.

[0088] Thus, oxygen and the initially gasified carbon dioxide will flow into the desulfurization device 17 through the heat exchange device, and the desulfurization device 17 will desulfurize the gas before transporting it to the reaction device 13, for example, the COS desulfurizer reacts with the COS contained in the carbon dioxide raw material to absorb COS before transporting it to the reaction device 13. The reacted material output from the reaction device 13 will flow into the second heat exchange channel 1502 after heat exchange with the aforementioned oxygen and the initially gasified carbon dioxide through the heat exchange device. In the heat exchange process, the oxygen and the initially gasified carbon dioxide absorb heat, and the reacted material absorbs cold, which is conducive to ensuring that the carbon dioxide is fully gasified, and is conducive to reducing the subsequent heating burden of the first heater 14, and improving the reaction efficiency during the desulfurization reaction, thereby improving the desulfurization effect.

[0089] Optionally, the carbon dioxide refining system further includes a second compressor 18. The inlet of the second compressor 18 is connected to the reaction outlet 1302, and the outlet is connected to the second heat exchange inlet 1603. As a result, when the reacted material flows through the second compressor 18, it will be pressurized and heated by the second compressor 18, so that oxygen and carbon dioxide can absorb more heat after passing into the heat exchange device 16, oxygen can be better heated, and carbon dioxide can be more fully gasified, which is conducive to further reducing the heating burden of the first heater 14, reducing energy consumption, and further improving the desulfurization effect.

[0090] Optionally, the carbon dioxide refining system further includes a cooling device 19 and an adsorption device 21. The cooling device 19 is connected to the rear stage of the reaction device 13. The adsorption device 21 is provided with a built-in adsorbent capable of absorbing water. And it is connected to the rear stage of the cooling device 19 and the front stage of the second heat exchange channel 1502. Thus, when the reacted material output from the reaction device 13 flows through the cooling device 19, the cooling device 19 cools the water vapor in the reacted material into a liquid phase. The liquid phase water vapor then flows through the adsorption device 21, and can be absorbed by the adsorbent more quickly, thereby quickly and fully removing the water vapor in the carbon dioxide raw material and the water vapor generated after the impurities in the reaction device 13 are removed.

[0091] Optionally, the cooling device 19 comprises a water cooler. The water cooler is used to reduce the temperature of the reacted material by heat exchange between cooling water and the reacted material, and has low cost.

[0092] Figure 3 Schematic diagram of the adsorption device 21 of the present disclosure in the first working state. Figure 1 and Figure 3 , the adsorption device 21 includes a first adsorber 211, a second adsorber 212, a regeneration gas input pipeline 213, a second heater 214 and a regeneration gas output pipeline 215. The second adsorber 212 and the first adsorber 211 are arranged in parallel, and both are provided with built-in adsorbent. The second heater 214 (such as an electric heater) is used to heat the regeneration gas transported by the regeneration gas input pipeline 213. And when one of the first adsorber 211 and the second adsorber 212 is connected to the reaction outlet 1302 and the inlet of the second heat exchange channel 1502, the regeneration gas input pipeline 213 is connected to the other of the first adsorber 211 and the second adsorber 212, so that when one of the first adsorber 211 and the second adsorber 212 performs adsorption work, the other can be heated by the introduced regeneration gas to regenerate the adsorbent and then output from the regeneration gas output pipeline 215. For example, Figure 3In the figure, the arrow shown on the dotted line passing through the second adsorber 212 indicates the flow direction of the regeneration gas flowing through the second adsorber 212, and the arrow shown on the dotted line passing through the first adsorber 211 indicates the flow direction of the carbon dioxide flowing through the first adsorber 211. Figure 3 When the first adsorber 211 performs adsorption operation, the second adsorber 212 is heated by the introduced regeneration gas to regenerate the adsorbent and then output it from the regeneration gas output pipeline 215, so that the adsorption device 21 can work continuously.

[0093] Figure 4 Schematic diagram of the adsorption device 21 of the present disclosure in the second working state. Figure 4 , the adsorption device 21 further includes a venting line 216. When one of the first adsorber 211 and the second adsorber 212 is connected to the reaction outlet 1302 and the inlet of the second heat exchange channel 1502, the venting line 216 is connected to the other of the first adsorber 211 and the second adsorber 212, so that when one of the first adsorber 211 and the second adsorber 212 performs adsorption, the reacted material introduced into the other is vented by the venting line 216. For example, Figure 4 In the figure, the arrow shown on the dotted line passing through the first adsorber 211 indicates the flow direction of the carbon dioxide flowing through the first adsorber 211, and the arrow on the dotted line drawn from the second adsorber 212 indicates the flow direction of the internal gas when the second adsorber 212 is emptied. Figure 4 In the embodiment, when the first adsorber 211 performs adsorption work and before the second adsorber 212 is regenerated, the reacted gas material stored in the second adsorber 212 is emptied and discharged. Thus, before the other adsorbent in the first adsorber 211 and the second adsorber 212 is regenerated, the reacted material stored in the other can be emptied to prevent the reacted material from affecting the regeneration of the adsorbent.

[0094] Optionally, the adsorption device 21 further includes first to tenth valves. Taking the first adsorber 211 performing adsorption work and the second adsorber 212 performing regeneration work as an example, refer to Figure 4 Before regeneration, the fourth valve d is closed and the eighth valve h is opened, so that the reacted material no longer flows into the second adsorber 212, and the reacted material that has been passed in can be emptied and discharged through the opened eighth valve h and the venting line 216. The third valve c is opened and the ninth valve i is opened, so that the reacted material can flow into the first adsorber 211 through the opened third valve c, and be discharged through the opened ninth valve i for adsorption.

[0095] During regeneration, see Figure 3 , the third valve c and the ninth valve i continue to remain open to allow the first adsorber 211 to continue adsorption. The sixth valve f and the second valve b are opened, so that the heated regeneration gas is introduced into the second adsorber 212 to allow the second adsorber 212 to regenerate.

[0096] Correspondingly, Figure 5 and Figure 6 Schematic diagram of the adsorption device 21 of the present disclosure in the third and fourth working states. Figure 5 Before regeneration, the fourth valve d and the tenth valve j are opened to allow the second adsorber 212 to perform adsorption. The third valve c is closed and the seventh valve g is opened to allow the first adsorber 211 to perform venting. In other words, Figure 5 In the figure, the arrow shown on the dotted line passing through the second adsorber 212 indicates the flow direction of the carbon dioxide flowing through the second adsorber 212, and the arrow on the dotted line drawn from the first adsorber 211 indicates the flow direction of the internal gas when the first adsorber 211 is emptied. Figure 5 When the second adsorber 212 performs adsorption and before the first adsorber 211 is regenerated, the post-reaction gas material stored in the first adsorber 211 is emptied and discharged.

[0097] See also Figure 6 During the regeneration process, the fourth valve d and the tenth valve j continue to remain open to allow the second adsorber 212 to continue adsorption. The fifth valve e and the first valve a are opened, so that the heated regeneration gas is introduced into the first adsorber 211 to perform regeneration. In other words, Figure 6 , the arrow shown on the dotted line passing through the first adsorber 211 indicates the flow direction of the regeneration gas flowing through the first adsorber 211 , and the arrow shown on the dotted line passing through the second adsorber 212 indicates the flow direction of the carbon dioxide flowing through the second adsorber 212 . Figure 6 When the second adsorber 212 performs adsorption, the first adsorber 211 is heated by the introduced regeneration gas to regenerate the adsorbent and then output it from the regeneration gas output pipeline 215, so that the adsorption device 21 can work continuously.

[0098] Optionally, see Figure 1, the carbon dioxide refining system further includes a reheat device 22. The reheat device 22 has a first reheat inlet 2201, a first reheat outlet 2202, a second reheat inlet 2203 and a second reheat outlet 2204. The first reheat inlet 2201 is connected to the reaction outlet 1302. The first reheat outlet 2202 is connected to the cooling device 19. The second reheat inlet 2203 is connected to the oxygen output port 1101 and the outlet of the first heat exchange channel 1501. The second reheat outlet 2204 is connected to the reaction inlet 1301. Thus, the reacted material output from the reaction outlet 1302 can be heat exchanged with the oxygen and gaseous carbon dioxide introduced into the reaction inlet 1301, so that the gas is preheated before the oxygen and gaseous carbon dioxide are input into the reaction inlet 1301 to reduce the heating burden of the first heater 14, and the reacted material is precooled before being transported to the cooling device 19 to reduce the cooling burden of the cooling device 19 and save energy.

[0099] The above embodiments are merely illustrative of the principles and effects of the present disclosure, and are not intended to limit the present disclosure. Anyone familiar with the technology may modify or change the above embodiments without violating the spirit and scope of the present disclosure. Therefore, all equivalent modifications or changes made by those with ordinary knowledge in the technical field without departing from the spirit and technical ideas disclosed in the present disclosure shall still be covered by the protection scope of the present disclosure.

Claims

1. A carbon dioxide refining system, characterized in that: include: an oxygen delivery device having an oxygen output port for outputting oxygen; A carbon dioxide delivery device having a carbon dioxide output port for outputting liquid carbon dioxide; A reaction device having a reaction inlet and a reaction outlet for reacting oxygen with impurities in carbon dioxide to form a reacted material; A first heater, provided in the reaction device or in the front stage of the reaction device, for heating the mixed oxygen and carbon dioxide; a heat exchange device, comprising a first heat exchange channel and a second heat exchange channel for heat exchange, wherein the inlet of the first heat exchange channel is connected to the carbon dioxide output port, the outlet of the first heat exchange channel is interconnected with the oxygen output port and connected to the reaction inlet, and the inlet of the second heat exchange channel is connected to the reaction outlet; and A distillation device is connected to the outlet of the second heat exchange channel, and is used for distilling and removing light impurities and heavy impurities in the reaction material after heat exchange; the distillation device includes: a first rectifier, having a first feed inlet, and the first feed inlet is connected to the outlet of the second heat exchange channel; a first reboiler, having a first reboiler inlet and a first reboiler outlet for coolant to flow in and out, respectively, for the refrigerant to flow and exchange heat with the liquid at the bottom of the first rectifier; a first condenser, having a first condensation inlet and a first condensation outlet, the first condensation inlet is connected to the first reboiler outlet, and is used for the reboiled refrigerant to flow and exchange heat with the gas at the top of the first condenser; and a first compressor, the inlet of which is connected to the first condensation outlet, and the outlet of which is connected to the first reboiler inlet; Wherein, the heat exchange device is provided with a third heat exchange channel capable of exchanging heat with the second heat exchange channel, and the inlet of the third heat exchange channel is connected to the outlet of the first rectifier for outputting heavy component impurities; and / or the heat exchange device is provided with a fourth heat exchange channel capable of exchanging heat with the second heat exchange channel, and the inlet of the fourth heat exchange channel is connected to the outlet of the first condenser for outputting condensed light component impurities.

2. The carbon dioxide purification system according to claim 1, characterized in that: The distillation device comprises: A second rectifier has a second feed inlet, wherein the second feed inlet is connected to a first discharge outlet at the top of the first rectifier; a second reboiler, arranged corresponding to the bottom of the second rectifier, and having a second reboiler inlet and a second reboiler outlet, wherein the second reboiler inlet is connected to the outlet of the first compressor and is used for the refrigerant to circulate and exchange heat with the liquid at the bottom of the second rectifier; A second condenser having a first cold inlet, a first cold outlet, a second cold inlet and a second cold outlet, wherein the first cold inlet is connected to the second reboiler outlet, the first cold outlet is connected to the inlet of the first compressor, and the second cold inlet and the second cold outlet are connected to the outlet and the inlet of the top of the second rectifier, respectively; The heat exchange device is provided with a fourth heat exchange channel capable of exchanging heat with the second heat exchange channel, and the inlet of the fourth heat exchange channel is connected to the second cold outlet.

3. The carbon dioxide refining system according to claim 2, characterized in that: The distillation device also includes: a subcooler, having a first subcooling inlet, a first subcooling outlet, a second subcooling inlet and a second subcooling outlet, the first subcooling inlet is connected to the second reboiler outlet, the first subcooling outlet is connected to the inlet of the first compressor, the second subcooling inlet is connected to the second heavy component outlet at the bottom of the second rectifier, and the second subcooling outlet is connected to a second storage container.

4. The carbon dioxide refining system according to claim 1, characterized in that: Also includes: a heat exchange device having a first heat exchange inlet, a first heat exchange outlet, a second heat exchange inlet and a second heat exchange outlet, wherein the first heat exchange inlet is connected to the oxygen output port and the outlet of the first heat exchange channel, the second heat exchange inlet is connected to the reaction outlet, and the second heat exchange outlet is connected to the inlet of the second heat exchange channel; The desulfurization device comprises a desulfurization inlet and a desulfurization outlet, wherein the desulfurization inlet is connected to the first heat exchange outlet, and the desulfurization outlet is connected to the reaction inlet.

5. The carbon dioxide purification system according to claim 4, characterized in that: Also includes: The second compressor has an inlet connected to the reaction outlet and an outlet connected to the second heat exchange inlet.

6. The carbon dioxide purification system according to claim 1, characterized in that: Also includes: A cooling device connected to the rear stage of the reaction device; The adsorption device contains a built-in adsorbent capable of absorbing water and is connected to the rear stage of the cooling device and the front stage of the second heat exchange channel.

7. The carbon dioxide purification system according to claim 6, characterized in that: The adsorption device comprises: The first adsorber; a second adsorber, arranged in parallel with the first adsorber; A regeneration gas input pipeline and a second heater, wherein the second heater is used to heat the regeneration gas transported by the regeneration gas input pipeline; and when one of the first adsorber and the second adsorber is connected to the reaction outlet and the inlet of the second heat exchange channel, the regeneration gas input pipeline is connected to the other of the first adsorber and the second adsorber.

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