CN220503214U - CO 2 Carbon negative device integrated with capturing electrolysis - Google Patents
CO 2 Carbon negative device integrated with capturing electrolysis Download PDFInfo
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- CN220503214U CN220503214U CN202321560370.1U CN202321560370U CN220503214U CN 220503214 U CN220503214 U CN 220503214U CN 202321560370 U CN202321560370 U CN 202321560370U CN 220503214 U CN220503214 U CN 220503214U
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- Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)
Abstract
The utility model discloses a CO 2 An integrated carbon negative device for trapping electrolysis, comprising: an electrolysis module comprising an electrolysis cell comprising a cathode chamber and an anode chamber; a cathode circulation module comprising a first input assembly and a first output assembly, wherein the first input assembly is suitable for conveying the rich liquid of the absorption liquid to the cathode chamber for cathode electrolysis reaction, and the first output assembly is suitable for conveying the rich liquid of the absorption liquid to the cathode chamberThe electrolytic reaction product and the absorption liquid lean solution are output in a split flow way, and the absorption liquid lean solution is fed with the supplementing solution and then is returned to CO 2 An absorption tower; the anode circulation module comprises a second input assembly and a second input assembly, the second input assembly is suitable for inputting an anode electrolyte to the anode chamber for electrolytic reaction, and the second output assembly is suitable for outputting an anode chamber electrolytic reaction product and a reacted electrolyte in a split way and inputting the reacted electrolyte back to the second input assembly. The utility model can directly electrolyze the rich liquid of the absorption liquid to obtain CO 2 Chemically utilizing the product and realizing rich liquor regeneration.
Description
Technical Field
The utility model relates to the technical field of carbon capture and utilization, in particular to a CO 2 And (3) capturing and electrolyzing the integrated carbon negative device.
Background
The industries of power generation, metallurgy, steel and the like can generate a large amount of CO 2 Emissions, causing environmental pollution and climate change. The CO emission reduction technology can effectively reduce CO emission 2 And thus is of great interest. CO capture by chemical absorption 2 The technology development is relatively mature and the separation effect is good, and especially the technology using organic amine as absorbent can be directly used for CO of flue gas in the scenes of coal-fired/gas-fired power plants, industrial boilers and the like 2 Emission reduction is realized, and the low-concentration CO has commercial prospect at present 2 Trapping technology. However, the rich liquid regeneration device has high energy consumption and high cost, and adds a barrier to the large-scale application of the chemical absorption technology. Furthermore, in the related art, the device design of carbon capture and utilization is mostly independent, and CO2 desorption or storage and transportation are required to be involved, which is disadvantageous for the cooperative coupling of the two processes to reduce construction, running and operation costs.
Disclosure of Invention
In view of the above problems, it is an object of the present utility model to provide a CO 2 The carbon negative device with integrated capturing and electrolysis can directly electrolyze the rich liquid of the absorption liquid to obtain CO 2 Chemical utilization of the product and realization of rich liquor regeneration (conversion to lean liquor) avoiding CO 2 Desorption and storage processes and associated energy consumption.
In order to achieve the above purpose, the present utility model adopts the following technical scheme:
CO (carbon monoxide) 2 An integrated carbon negative device for trapping electrolysis, comprising: an electrolysis module comprising an electrolysis cell comprising a cathode chamber and an anode chamber; a cathode circulation module comprising a first input assembly and a first output assembly, the first input assembly being adapted to convert CO 2 The absorption liquid rich solution of the absorption tower is conveyed to the cathode chamber for cathode electrolytic reaction, the first output component is suitable for shunting and outputting an absorption liquid lean solution formed after the cathode chamber electrolytic reaction product and the electrolytic reaction, and the absorption liquid lean solution is fed with the supplementing liquid and then conveyed back to the CO 2 An absorption tower; the anode circulation module comprises a second input assembly and a second output assembly, wherein the second input assembly is suitable for inputting an anode electrolyte to the anode chamber for electrolytic reaction, the second output assembly is suitable for outputting an anode chamber electrolytic reaction product and a reacted electrolyte in a split way, and the reacted electrolyte is returned to the second input assembly.
According to at least one embodiment of the present utility model, the first input assembly comprises: the first pump is arranged on the pipeline of the first input assembly for conveying the absorption liquid rich liquid and is suitable for driving the absorption liquid rich liquid to flow and adjusting the pressure of the absorption liquid rich liquid; and the first pressure sensor is arranged in a pipeline between the first pump and the cathode chamber and is suitable for detecting the pressure of the absorption liquid rich liquid.
According to at least one embodiment of the present utility model, the first input assembly further comprises: a first valve arranged between the first pump and the CO 2 A pipeline between the absorption towers; and the first buffer tank is arranged on a pipeline between the first valve and the first pump.
According to at least one embodiment of the present utility model, the first output assembly includes a first separator, a first mixer, a second pump and a second buffer tank, which are sequentially connected, the first separator is connected to the output pipeline of the cathode chamber to split and output the electrolysis reaction product of the cathode chamber and the lean solution of the absorption solution, the first mixer is bypassed and connected to a second valve and a supplementary solution input pipeline controlled by the second valve, the first mixer is adapted to supply the supplementary solution to the lean solution of the absorption solution, the second pump is adapted to drive the lean solution of the absorption solution and the flow of the supplementary solution downstream of the first mixer, the second buffer tank is provided with a first liquid level detection device, the first liquid level detection device is electrically connected to the second valve, and the output end of the second buffer tank is adapted to output the lean solution of the absorption solution to the CO2 absorption tower.
According to at least one embodiment of the utility model, the first output assembly comprises a detection device adapted to detect a composition of a stream of the electrolytic reaction product of the cathodic compartment, the detection device being bypass connected to the output line of the cathodic compartment and electrically connected to the first valve.
According to at least one embodiment of the present utility model, the second input assembly includes: the third pump is arranged on the pipeline of the second input assembly for conveying the anolyte, and is suitable for driving the anolyte to flow and adjusting the pressure of the anolyte; and the second pressure sensor is arranged on a pipeline between the third pump and the anode chamber and is suitable for detecting the pressure of the anolyte.
According to at least one embodiment of the present utility model, the second input assembly further comprises: the third valve is arranged on an anode electrolyte input pipeline connected with the third pump; the second mixer is arranged in a pipeline between the third pump and the third valve and is connected with the second output assembly to receive the electrolyte after reaction; the third buffer tank is provided with a second liquid level detection device electrically connected with the third valve; and the heater is arranged in a pipeline between the third pump and the anode chamber and is suitable for heating the temperature of the anolyte to be matched with the temperature of the liquid in the cathode chamber.
According to at least one embodiment of the present utility model, the second output assembly comprises a second separator, an input end of the second separator is connected to an output pipeline of the anode chamber, an output end of the second separator is connected to the second mixer through a pipeline to return the electrolyte after reaction to the second input assembly, and the other output end of the second separator is suitable for outputting the electrolytic reaction product of the anode chamber.
According to at least one embodiment of the utility model, the electrolytic cells are configured as a plurality of series, parallel or series-parallel connection, the electrolytic reaction products of the anode chambers of the plurality of second separators are suitable for being output through the same third mixer, each second separator is suitable for outputting the electrolyte after reaction to the anode chamber of the electrolytic cell at the downstream thereof, the anode chamber at the head end of the stroke is connected with the second input assembly, the second separator connected with the anode chamber at the tail end of the stroke is suitable for outputting the electrolytic reaction products of the cathode chambers and the absorbing liquid lean liquid after reaction back to the second mixer, the cathode chambers of the plurality of electrolytic cells are suitable for being connected with the first input assembly, and the cathode chamber at the head end of the stroke is connected with the cathode chamber at the tail end of the stroke through the first separator.
According to at least one embodiment of the utility model, the CO 2 The integrated carbon negative device for capturing and electrolyzing also comprises a content forming containerThe shell of accommodation space, electrolytic module locates in the middle of the accommodation space, one side wall body of shell sets up positive pole electrolyte entry, absorption liquid rich solution entry, absorption liquid lean solution export and supplementary liquid entry, and another opposite side wall body sets up positive pole room electrolytic reaction product export and negative pole room electrolytic reaction product export.
In accordance with at least one embodiment of the present utility model, a tortuous and extended cathode chamber flow passage is formed in the cathode chamber for the absorption rich liquid to flow through and react with the cathode catalyst, and a tortuous and extended anode chamber flow passage is formed in the anode chamber for the anolyte to flow through and react with the anode catalyst.
According to at least one embodiment of the present utility model, the absorbent in the absorbent solution is an amine compound including monoethanolamine, N-diethylethanolamine, methyldiethanolamine, 1-dimethylamino-2-propanol, tetraethylenepentamine, triethylenetetramine, ethylenediamine, N-methyldiethanolamine, 2-amino-2-methyl-1-propanol, 4-diethylamino-2-butanol, diethylenetriamine, and/or diethylaminoethanol, or a basic inorganic compound including KOH, naOH, and/or KHCO 3 。
According to at least one embodiment of the present utility model, the concentration of the absorbent compound in the absorption liquid is selected from the range of 0.05mol/L to 10mol/L.
According to at least one embodiment of the present utility model, the concentration of the absorbent compound in the absorption liquid is selected from the range of 1mol/L to 5mol/L.
According to at least one embodiment of the utility model, the power source for providing the electrical energy required by the electrolytic cell comprises wind power, photovoltaic power generation and the power of the mains trough.
According to at least one embodiment of the utility model, the CO 2 The integrated carbon negative device for capturing electrolysis further comprises a product treatment module for producing carbon utilization products, wherein the product treatment module comprises a separation and purification device for separating and purifying the cathode chamber electrolysis reaction products and/or the anode chamber electrolysis reaction products.
According to the present utility modelAt least one embodiment of the utility model is configured as a membrane separation device adapted to receive the cathode chamber electrolytic reaction product to separate and purify H in the cathode chamber electrolytic reaction product component 2 。
According to at least one embodiment of the utility model, the cathode chamber is separated from the anode chamber by an ion exchange membrane.
Due to the adoption of the technical scheme, the utility model has at least the following advantages:
1. CO 2 The absorption tower, the first input component, the cathode chamber and the first output component form CO 2 The system for circulating the absorption liquid comprises a first input component, a cathode chamber electrolysis reaction product and an absorption liquid lean solution, wherein the cathode chamber electrolysis reaction product and the absorption liquid lean solution are generated after the absorption liquid rich solution is input into a cathode chamber for electrolysis reaction, the absorption liquid lean solution is shunted and output by the first output component, and the absorption liquid lean solution is input back to CO after the supplementing liquid is supplemented 2 An absorption tower; the second input assembly, the anode chamber and the second output assembly form a circulating flow system of the anode electrolyte, the second input assembly is suitable for being connected with an electrolyte source outside the circulating system to continuously supplement enough anode electrolyte, the second input assembly inputs the anode electrolyte into the anode chamber to carry out electrolytic reaction, then an anode chamber electrolytic reaction product generated after the electrolytic reaction and the reacted electrolyte are shunted and output by the second output assembly, and the reacted electrolyte is returned to the first input assembly to be mixed with the newly input anode electrolyte and then can be continuously conveyed to the anode chamber to carry out electrolytic reaction;
2. the CO provided by the utility model 2 The integrated carbon negative device system for capturing and electrolyzing has high integration level, can realize the conversion and utilization of CO2 and the regeneration of rich liquid at the same time, omits the steps of CO2 desorption, storage, transportation and the like, saves the energy consumption of related equipment such as a reboiler, a cooler and the like, and simultaneously, the working temperature range of the device is matched with the inlet and outlet temperatures of an upstream absorption tower, thereby avoiding complex heat matching processes such as heat exchange and the like;
3. the CO provided by the utility model 2 The control precision of the carbon negative device integrated with the capturing and electrolysis is high, and the starting, stopping and proceeding degree of the reaction can be directly controlled through an electric signal;
4. the CO provided by the utility model 2 The integrated carbon negative device for capturing and electrolyzing can be suitable for the power of renewable energy sources such as wind power, photovoltaic power generation and the like and the power of a power grid trough, and the carbon dioxide is changed into valuable by adopting low-cost power;
5. the CO provided by the utility model 2 The integrated carbon negative device for capturing and electrolyzing can realize various and adjustable CO2 conversion products by changing electrolysis reaction conditions and catalyst types, and provides various directions for downstream CO2 resource utilization.
Drawings
FIG. 1 is a schematic diagram of CO in at least one embodiment of the utility model 2 Schematic structural diagram of an integrated carbon negative device for capturing electrolysis;
FIG. 2 is a schematic diagram of CO in at least one embodiment of the utility model 2 Schematic structural diagram of an integrated carbon negative device for capturing electrolysis;
FIG. 3 is a diagram of CO in at least one embodiment of the utility model 2 A shell structure schematic diagram of an electrolysis-trapping integrated carbon negative device;
FIG. 4 is a schematic diagram of CO in at least one embodiment of the utility model 2 The flow channel structure of the integrated carbon negative device for capturing and electrolyzing (2 a refers to a snake-shaped flow channel and 2b refers to a penetrating flow channel).
The reference numerals in the drawings:
a is an absorption liquid rich liquid inlet; b is an absorption liquid lean liquid outlet; c is a make-up liquid inlet; d is the outlet of the electrolytic reaction product of the cathode chamber; e is the outlet of the electrolytic reaction product of the anode chamber; f is the anolyte inlet;
1 is a first buffer tank; 2 is a first pump; 3 is a cathode chamber; 4 is a first shunt; 5 is a first mixer; 6 is a second pump; 7 is a second buffer tank; 8 is a second mixer; 9 is a third buffer tank; 10 is a third pump; 11 is a heater; 12 is an anode chamber; 13 is a second splitter; 14 is a third mixer;
3-1, 3-2, … …, and 3-N are cathode chambers connected in series;
v1 is a first valve; v2 is a second valve; v3 is a third valve;
p-1 is a first pressure sensor, and P-2 is a second pressure sensor; the AP is a detection device.
Detailed Description
In order to make the objects, technical solutions and advantages of the present utility model more apparent, the technical solutions of the present utility model will be clearly and completely described below with reference to the accompanying drawings. It will be apparent that the described embodiments are some, but not all, embodiments of the utility model. All other embodiments, which can be made by those skilled in the art based on the embodiments of the utility model without making any inventive effort, are intended to be within the scope of the utility model.
In the description of the present utility model, it should be noted that the azimuth or positional relationship indicated by the terms "upper", "lower", "front", "rear", etc. are based on the azimuth or positional relationship shown in the drawings, and are merely for convenience of describing the present utility model and simplifying the description, and do not indicate or imply that the system or element referred to must have a specific azimuth, be configured and operated in a specific azimuth, and thus should not be construed as limiting the present utility model.
In the description of the present utility model, it should be noted that, unless explicitly stated and limited otherwise, the terms "mounted," "disposed," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; the mechanical connection and the electrical connection can be adopted; can be directly connected or indirectly connected through an intermediate medium, and can be communication between two elements. The specific meaning of the above terms in the present utility model will be understood in specific cases by those of ordinary skill in the art.
In view of the technical problems in the background art, the utility model provides a CO 2 Carbon-negative device with integrated carbon capturing and electrolysis, capable of realizing high integration of carbon capturing and utilization, and CO 2 The carbon negative device integrated with the capturing electrolysis can directly electrolyze CO 2 The rich liquid of the absorption liquid output by the absorption tower obtains CO 2 Chemical utilization of the product and realization of rich liquid regeneration, avoiding CO 2 The desorption and storage and transportation processes can be suitable for the electric power of renewable energy sources such as wind power, photovoltaic power generation and the like,CO using inexpensive electricity 2 Changing waste into valuables.
CO at present 2 The market capacity of the product is limited, the added value of the product is small, and the popularization of the carbon trapping related technology is greatly limited. In recent years, CO 2 Chemical immobilization of (c) has received much attention as an effective resource utilization route. The CO provided by the utility model 2 The carbon negative device integrated with the trapping electrolysis can trap CO 2 Converted into alkane, formaldehyde, ethylene, alcohol and other products to solve the problem of CO 2 The difficult problem of high value-added utilization improves the economy of the carbon emission reduction project. In a plurality of COs 2 In the new technology of conversion, electrochemical catalysis of CO 2 Conversion, inert CO can be activated efficiently by means of electricity 2 The molecule has stronger advantages in the aspects of early equipment investment and operation cost.
The CO provided by the embodiment of the utility model is as follows with reference to the accompanying drawings 2 The integrated carbon negative device for collecting and electrolyzing will be described in detail.
Example 1:
referring to FIGS. 1 through 3, a CO according to an embodiment of the present utility model 2 The carbon negative device integrated with the capturing electrolysis comprises an electrolysis module, a cathode circulation module and an anode circulation module. Wherein the electrolysis module comprises an electrolysis cell comprising a cathode chamber 3 and an anode chamber 12; the cathode circulation module comprises a first input assembly and a first output assembly, the first input assembly being adapted to convert CO 2 The rich liquid of the absorption tower is conveyed to the cathode chamber 3 for cathode electrolytic reaction, the first output component is suitable for shunting and outputting the product of the cathode chamber electrolytic reaction and the lean liquid of the absorption liquid formed after the electrolytic reaction, and the supplementing liquid is fed back to CO after supplementing the lean liquid of the absorption liquid 2 An absorption tower; the anode circulation module includes a second input assembly adapted to input anolyte to the anode chamber 12 for electrolytic reaction, and a second output assembly adapted to split output of the anode chamber electrolytic reaction product and reacted electrolyte and to return the reacted electrolyte to the second input assembly.
In the present embodiment, CO 2 Absorption tower, first input assembly, cathode chamber 3 and first output setPart formation CO 2 The system for circulating and flowing the absorption liquid comprises a first input component, a cathode chamber electrolytic reaction product and an absorption liquid lean solution, wherein the cathode chamber electrolytic reaction product and the absorption liquid lean solution are generated after the absorption liquid rich solution is input into a cathode chamber 3 for electrolytic reaction, the absorption liquid lean solution is shunted and output by a first output component, and the absorption liquid lean solution is input back to CO after being supplemented with the supplementing liquid 2 An absorption tower; the second input assembly, the anode chamber 12 and the second output assembly form a circulating flow system of the anolyte, the second input assembly is suitable for being connected with an electrolyte source outside the circulating system to continuously supplement enough anolyte, the second input assembly inputs the anolyte into the anode chamber 12 to carry out electrolysis reaction, then the generated anode chamber electrolysis reaction product and the reacted electrolyte are shunted and output by the second output assembly, and the reacted electrolyte is input back to the first input assembly to be mixed with the newly input anolyte and then can be continuously input into the anode chamber 12 to carry out electrolysis reaction.
Optionally, referring to fig. 1 and 2, the first input assembly includes a first pump 2 and a first pressure sensor P-1, where the first pump 2 is disposed on a pipeline of the first input assembly for conveying the rich liquid of the absorption liquid, and is adapted to drive the flow of the rich liquid of the absorption liquid and adjust the pressure of the rich liquid of the absorption liquid; the first pressure sensor P-1 is provided in the line between the first pump 2 and the cathode chamber 3, and is adapted to detect the pressure of the rich absorption liquid. The first pressure sensor P-1 can detect the pressure of the rich absorbent liquid, and the power of the first pump 2 can be adjusted according to the detection data to perform pressure adjustment on the rich absorbent liquid, so that the pressure of the rich absorbent liquid is matched with the working pressure of the cathode chamber 3 and the whole device.
Further, referring to fig. 1 and 2, the first input assembly further includes a first valve V1 and a first buffer tank 1, the first valve V1 is disposed between the first pump 2 and the CO 2 A pipeline between the absorption towers; the first buffer tank 1 is arranged in a pipeline between the first valve V1 and the first pump 2. CO-enriched from upstream chemical carbon capture process stage 2 The absorption liquid rich liquid enters the first buffer tank 1 through the first valve V1 to stabilize the pressure, and then flows into the cathode chamber 3 of the electrolytic cell to carry out cathode electrolytic reaction under the action of the first pump 2.
Optionally, referring to fig. 1 and 2, the first output assembly includes a first separator 4, a first mixer 5, a second pump 6 and a second buffer tank 7 that are sequentially connected, the first separator 4 is connected to an output pipeline of the cathode chamber 3 to split and output an electrolysis reaction product and an absorption liquid lean solution in the cathode chamber, the first mixer 5 is bypass-connected to a second valve V2 and a supplementary liquid input pipeline controlled by the second valve V2, the first mixer 5 is suitable for supplying the supplementary liquid to the absorption liquid lean solution, the second pump 6 is suitable for driving the absorption liquid lean solution and the supplementary liquid to flow downstream of the first mixer 5, the second buffer tank 7 is provided with a first liquid level detection device AP and the first liquid level detection device AP is electrically connected to the second valve V2, and an output end of the second buffer tank 7 is suitable for outputting the absorption liquid lean solution to the CO2 absorption tower.
After the electrolysis reaction, the absorption liquid rich solution is converted into the absorption liquid lean solution to realize regeneration, and the absorption liquid lean solution and the cathode chamber electrolysis reaction product are split into two paths through the first separator 4. The converted absorption liquid lean liquid flows out of the cathode chamber 3 of the electrolytic cell. Meanwhile, the replenishing liquid for replenishing the lean liquid of the absorption liquid is conveyed to the first mixer 5 for mixing through the second valve V2, and the flow rate of the replenishing liquid can be controlled by the second valve V2. The lean solution of the absorption liquid and the supplementary solution are mixed by the first mixer 5 and then are pressurized by the second pump 6 to enter the second buffer tank 7. The liquid level in the second buffer tank 7 is measured, and the replenishment flow rate of the replenishment liquid is controlled based on the measurement data. The mixed liquid formed by the lean liquid of the absorption liquid and the supplementary liquid is output and recycled back to CO flowing into the upstream 2 The absorption tower, and the cathode chamber electrolysis reaction product can flow out of the circulation system after being split.
Further, referring to fig. 1 and 2, the first output assembly includes a detecting device AP adapted to detect a flow component of the electrolytic reaction product in the cathode chamber, and the detecting device AP is bypass connected to the output line of the cathode chamber 3 and electrically connected to the first valve V1. By detecting the material flow components of the cathode chamber electrolytic reaction product output by the cathode chamber 3, the electrolytic reaction conversion rate can be clarified, and the flow of the absorption liquid rich liquid entering the first input assembly through the first valve V1 is correspondingly regulated so as to ensure the full regeneration of the absorption liquid rich liquid in the electrolytic reaction process.
Optionally, referring to fig. 1 and 2, the second input assembly includes a third pump 10 and a second pressure sensor P-2, where the third pump 10 is disposed on a pipeline of the second input assembly for delivering the anolyte, and is adapted to drive the anolyte to flow and regulate the pressure of the anolyte; the second pressure sensor P-2 is arranged in the line between the third pump 10 and the anode chamber 12 and is adapted to detect the pressure of the anolyte. The second pressure sensor P-2 is capable of detecting the anolyte pressure, and based on the detected data, the power of the third pump 10 can be adjusted to pressure-adjust the anolyte so that the anolyte pressure matches the operating pressure of the anode chamber 12 and the entire apparatus.
Optionally, referring to fig. 1 and 2, the second input assembly further includes: the third valve V3, the second mixer 8, the third buffer tank 9 and the heater 11 are arranged on an anolyte input pipeline connected with the third pump 10; the second mixer 8 is arranged in a pipeline between the third pump 10 and the third valve V3, and is connected with the second output assembly to receive the electrolyte after reaction; the third buffer tank 9 is provided with a second liquid level detection device AP electrically connected with a third valve V3; a heater 11 is provided in the line between the third pump 10 and the anode chamber 12 and is adapted to heat the anolyte temperature to match the liquid temperature in the cathode chamber 3.
The externally replenished anolyte enters the anode circulation module through a third valve V3 and the reacted electrolyte returned by the second output assembly is mixed through a second mixer 8. Thereafter, the mixed anolyte enters the third pump 10, continues to circulate under the drive of the third pump 10, and enters the third buffer tank 9 during the flowing process, the liquid level in the third buffer tank 9 is measured by the second liquid level detection device AP, and the flow rate of the anolyte replenished through the third valve V3 is controlled according to the detection data. The anolyte then enters the heater 11 to be heated to a temperature matching the absorption liquid in the cathode chamber 3 and then enters the anode chamber 12 of the electrolytic cell for electrolytic reaction. And the electrolyte and the electrolytic reaction product of the anode chamber flow out of the electrolytic cell together after the reaction.
Further, referring to fig. 1 and 2, the second output assembly includes a second separator 13, an input end of the second separator 13 is connected to an output pipeline of the anode chamber 12, an output end is connected to the second mixer 8 through a pipeline to return the reacted electrolyte to the second input assembly, and another output end is adapted to output an electrolytic reaction product in the anode chamber. In this embodiment, the reacted electrolyte and the product of the electrolytic reaction in the anode chamber are split into two streams of gas and liquid by the second separator 13, and the oxygen generated by the electrolytic reaction is split and output outside the circulating system boundary, and the reacted electrolyte is returned to the second mixer 8 and mixed with the externally supplied anolyte.
Without loss of generality, referring to fig. 2, the electrolytic cells are configured as a plurality of series, parallel or series-parallel, anode chamber electrolytic reaction products branched by a plurality of second separators 13 are suitable for being output through the same third mixer 14, each second separator 13 is suitable for outputting the reacted electrolyte to the anode chamber 12 of the electrolytic cell downstream thereof, the anode chamber 12 at the head end of the stroke is connected with a second input assembly, the second separator 13 connected with the anode chamber 12 at the tail end of the stroke is suitable for inputting the reacted electrolyte back to the second mixer 8, the cathode chambers 3 of the plurality of electrolytic cells are suitable for being connected, and the cathode chamber 3-1 at the head end of the stroke is connected with a first input assembly, and the cathode chamber 3-N at the tail end of the stroke is branched for outputting the cathode chamber electrolytic reaction products and the absorption liquid lean liquid through the first separator 4. Thus, a plurality of electrolytic cells can be connected in series, parallel or series-parallel to form a multi-layer electrolytic module system.
Alternatively, referring to fig. 1 to 3, CO 2 The integrated carbon negative device for capturing and electrolyzing also comprises a shell with a containing space formed therein, the electrolysis module is arranged in the middle of the containing space, one side wall body of the shell is provided with an anode electrolyte inlet f, an absorbing liquid rich liquid inlet a, an absorbing liquid lean liquid outlet b and a supplementing liquid inlet c, and the other opposite side wall body is provided with an anode chamber electrolysis reaction product outlet e and a cathode chamber electrolysis reaction product outlet d. Specifically, externally replenished anolyte enters the second input assembly through anolyte inlet f, CO 2 The rich liquid of the absorption tower enters the first input assembly through the rich liquid inlet a of the absorption liquid, the supplementary liquid enters the first output assembly through the supplementary liquid inlet c, and the mixed liquid formed by the lean liquid of the absorption liquid and the supplementary liquid is returned to the CO through the lean liquid outlet b of the absorption liquid 2 An absorption tower. It will be appreciated that the individual modules areThe device is arranged in the same shell, so that the high integration of the device can be realized.
Alternatively, referring to fig. 4, a meandering cathode chamber flow passage is formed in the cathode chamber 3 for the rich absorbent solution to flow therethrough and react with the cathode catalyst, and a meandering anode chamber flow passage is formed in the anode chamber 12 for the anolyte solution to flow therethrough and react with the anode catalyst. In this way, the contact between the cathode catalyst and the rich absorbent solution and the contact between the anode catalyst and the anolyte can be enhanced, and the CO can be enhanced 2 The conversion rate in the single-pass flow ensures the full regeneration of the rich liquid of the absorption liquid. Illustratively, the cathode chamber flow channels and/or the anode chamber flow channels are provided as serpentine flow channels or interspersed flow channels.
Optionally, the absorbent in the absorption liquid adopts amine compound or basic inorganic compound, wherein the amine compound comprises monoethanolamine, N-diethyl ethanolamine, methyldiethanolamine, 1-dimethylamino-2-propanol, tetraethylenepentamine, triethylenetetramine, ethylenediamine, N-methyldiethanolamine, 2-amino-2-methyl-1-propanol, 4-diethylamino-2-butanol, diethylenetriamine and/or diethylaminoethanol, and the basic inorganic compound comprises KOH, naOH and/or KHCO 3 . That is, the amine compound may be one or more of monoethanolamine, N-diethylethanolamine, methyldiethanolamine, 1-dimethylamino-2-propanol, tetraethylenepentamine, triethylenetetramine, ethylenediamine, N-methyldiethanolamine, 2-amino-2-methyl-1-propanol, 4-diethylamino-2-butanol, diethylenetriamine and diethylaminoethanol, and the basic inorganic compound may be KOH, naOH and KHCO 3 One or a mixture of more than two of them.
On the surface of the cathode of the electrolytic cell, the absorbent and CO are directly electrolyzed 2 A compound formed by binding. The amine compound in the absorbent is used as R 1 R 2 NH、CO 2 The electrolytic conversion product is CO as an example, and the absorption liquid rich liquid direct electrolytic reaction occurring in the cathode chamber 3 is as follows:
R 1 R 2 NH+COO - +2e - +H 2 O→CO+2OH - +R 1 R 2 NH
further, the concentration of the absorbent compound in the absorbent solution is selected from the range of 0.05mol/L to 10mol/L. That is, the concentration of the absorbent compound in the absorbent liquid may be 0.05mol/L, 1mol/L, 2mol/L, 3mol/L, 4mol/L, 5mol/L, 6mol/L, 7mol/L, 8mol/L, 9mol/L, 10mol/L, or other values in the range of 0.05mol/L to 10mol/L.
Further, the concentration of the absorbent compound in the absorbent solution is selected from the range of 1mol/L to 5mol/L. That is, the concentration of the absorbent compound in the absorbent liquid may be 1mol/L, 2mol/L, 3mol/L, 4mol/L, 5mol/L, or other values in the range of 1mol/L to 5mol/L.
Alternatively, referring to fig. 1 and 2, the power source for providing the electrical energy required by the electrolytic cell includes, but is not limited to, wind power, photovoltaic power generation, and power from a mains electricity sink.
Optionally, CO 2 The integrated carbon negative device for capturing and electrolyzing also comprises a product treatment module for producing carbon utilization products, wherein the product treatment module comprises a separation and purification device which is used for separating and purifying cathode chamber electrolytic reaction products and/or anode chamber electrolytic reaction products.
Alternatively, the separation and purification device is configured as a membrane separation device adapted to receive the cathode chamber electrolytic reaction product to separate and purify the H in the cathode chamber electrolytic reaction product component 2 . Illustratively, when the electrolytic cell is powered using renewable energy sources, the products are CO and H 2 When the membrane separation device is connected with the output end of the first separator 4, the cathode chamber electrolytic reaction product separated by the first separator 4 is delivered to the membrane separation device to purify H in the component 2 I.e. in realizing CO 2 Green hydrogen can be produced while electrochemical conversion and rich liquor regeneration are performed.
Alternatively, referring to fig. 1 and 2, the cathode chamber 3 is separated from the anode chamber 12 by an ion exchange membrane.
Example 2:
referring to fig. 1 to 4, the present embodiment provides a novel CO 2 The integrated device mainly comprises an electrolysis module, a cathode circulation module, an anode circulation module and a product treatment module.
Illustratively, with monoethanolamine as the absorbent, the absorption liquid rich liquid from the upstream chemical process carbon capture process enters the cathode circulation module from the absorption liquid rich liquid inlet a at a pressure of about 20kPag to 50kPag and a temperature of about 50 ℃; the electrolyte enters the first buffer tank 1 through the first valve V1 to stabilize the pressure, and then flows into the electrolytic cell cathode chamber 3 of the electrolytic module under the action of the first pump 2. The cell cathode chamber 3 uses an Ag-based catalyst to energize the electrolytic reaction with a renewable energy source. After the electrolysis reaction, the rich absorption liquid is converted into lean absorption liquid to realize regeneration; conversion of carbon dioxide to electrolysis products CO and H 2 The method comprises the steps of carrying out a first treatment on the surface of the The two are split into two paths of gas and liquid through the first separator 4. By detecting the material flow components of the electrolytic reaction product in the cathode chamber, the conversion rate of the electrolytic reaction can be clarified, and the flow rate of the rich liquid of the inlet absorption liquid can be correspondingly regulated so as to ensure the rich liquid to be fully regenerated. The converted absorption liquid lean liquid flows out of the cathode chamber 3 of the electrolytic cell. Meanwhile, the supplemented absorption liquid flows in through the supplemented liquid inlet c, the flow rate is controlled by the second valve V2, and after being mixed by the first mixer 5, the absorption liquid is pressurized to about 50kPag through the second pump 6 and enters the second buffer tank 7. Alternatively, the flow rate of the replenishment liquid is controlled by measuring the liquid level of the second buffer tank 7. The mixed liquid of the absorption liquid lean liquid and the supplementing liquid is finally output from the absorption liquid lean liquid outlet b and flows back into CO 2 The temperature of the absorption tower is about 40-50 ℃. Electrolysis products CO and H 2 The purified and refined product flows out of the boundary of the circulating system from the outlet d of the electrolytic reaction product of the cathode chamber, can be used as a fuel to be mixed with fuel gas to optimize the power generation cycle of a fuel gas power plant, and can be used as a raw material for further preparing high-added-value chemicals (such as methanol, oil products and the like); h can also be added by membrane separation device 2 Separated to produce green hydrogen.
The anode chamber 12 is subjected to oxygen evolution reaction, the anode catalyst is foamed nickel coated with Ru, pd and Pt, and the anolyte is potassium hydroxide solution with the concentration of 0.5 mol/L. The externally-replenished anolyte enters the anode circulation module from the anolyte inlet f, and is mixed with the reacted anolyte in the anode circulation module through the second mixer 8 after passing through the third valve V3. Thereafter, the mixed anolyte enters the third pump 10 and continues to flow under the drive of the third pump 10 into the third buffer tank 9. By measuring the liquid level in the third buffer tank 9, the flow rate of the externally supplied anolyte is controlled. The anolyte then enters heater 11 to be heated to 50 c and then enters the cell anode chamber 12 of the electrolysis module. The electrolyte after reaction and the electrolytic reaction product of the anode chamber flow out of the anode chamber 12 together, are split into two streams of gas and liquid by a second separator 13, oxygen generated by the electrolytic reaction flows out of the system boundary from an outlet e of the electrolytic reaction product of the anode chamber, and the electrolyte after reaction is circulated into a second mixer 8 to be mixed with the anode electrolyte which is replenished from the outside. Alternatively, the oxygen-enriched anode outlet gas may be combined with air required for power generation by the combustion engine, enhancing the efficiency of the combustion engine.
Example 3:
as shown in fig. 2 to 4, a plurality of electrolytic cells are connected in series, the Cu-based catalyst is used in the cathode chamber 3 of the electrolytic cell, the device is powered by renewable energy, and alternate flow channels are selected to enhance the contact of the electrocatalyst with the rich liquid of the absorption liquid, so that the conversion rate of the rich liquid in the cathode chamber 3 of the single electrolytic cell can be improved. After the electrolysis reaction, a part of the absorption liquid rich liquid is converted into lean liquid; a part of CO 2 Is converted into methanol as an electrolysis product. The liquid flowing out from the cathode chamber 3 of the electrolytic cell at the upper stage can enter the cathode chamber 3 of the electrolytic cell at the lower stage in series connection, and the reaction is continued under similar conditions, so that the enrichment of methanol and the full regeneration of rich liquid are realized. In addition, by detecting the flow components of the electrolytic reaction product in the cathode chamber, the conversion rate of the electrolytic reaction can be clarified, and the flow of the rich liquid of the absorption liquid input by the first input component is correspondingly regulated so as to ensure the rich liquid to be fully regenerated. The liquid exiting the cell cathode chamber 3 at the end of the stroke is split into two streams by a first separator 4: methanol and regenerated absorption liquid lean liquid. The methanol is purified by infiltration, rectification and other devices. The supplemented absorption liquid flows in through the supplemented liquid inlet c, the flow rate is controlled by the second valve V2, and after being mixed by the first mixer 5, the supplemented absorption liquid enters the second buffer tank 7 through the pressurization of the second pump 6. The flow rate of the replenishment liquid is controlled by measuring the liquid level in the second buffer tank 7. The mixed liquid of the absorption liquid lean liquid and the supplementing liquid is finally output from the absorption liquid lean liquid outlet b and flows backCO in 2 An absorption tower.
The anode chamber 12 is subjected to oxygen evolution reaction, the anode catalyst is foamed nickel coated with Ru, pd and Pt, and the anolyte is potassium hydroxide solution with the concentration of 0.5 mol/L. The flow path of the anolyte passes in series through the anode chambers 12 of a plurality of electrolytic cells where the oxygen product of the electrolytic reaction in the anode chambers 12 is collected in the manner shown in fig. 3. The other portions are the same as in example 2.
It should be noted that "and/or" in the whole text includes three schemes, taking "a and/or B" as an example, including a technical scheme, a technical scheme B, and a technical scheme that a and B meet simultaneously.
Finally, it should be noted that: the above embodiments are only for illustrating the technical solution of the present utility model, and are not limiting; although the utility model has been described in detail with reference to the foregoing embodiments, it will be understood by those of ordinary skill in the art that: the technical scheme described in the foregoing embodiments can be modified or some technical features thereof can be replaced by equivalents; such modifications and substitutions do not depart from the spirit and scope of the technical solutions of the embodiments of the present utility model.
Claims (10)
1. CO (carbon monoxide) 2 The integrated carbon negative device of entrapment electrolysis, characterized by comprising:
an electrolysis module comprising an electrolysis cell comprising a cathode chamber and an anode chamber;
a cathode circulation module comprising a first input assembly and a first output assembly, the first input assembly being adapted to convert CO 2 The absorption liquid rich solution of the absorption tower is conveyed to the cathode chamber for cathode electrolytic reaction, the first output component is suitable for shunting and outputting an absorption liquid lean solution formed after the cathode chamber electrolytic reaction product and the electrolytic reaction, and the absorption liquid lean solution is fed with the supplementing liquid and then conveyed back to the CO 2 An absorption tower;
the anode circulation module comprises a second input assembly and a second output assembly, wherein the second input assembly is suitable for inputting an anode electrolyte to the anode chamber for electrolytic reaction, the second output assembly is suitable for outputting an anode chamber electrolytic reaction product and a reacted electrolyte in a split way, and the reacted electrolyte is returned to the second input assembly.
2. The CO according to claim 1 2 The integrated carbon negative device for capturing and electrolyzing is characterized in that,
the first input assembly includes:
the first pump is arranged on the pipeline of the first input assembly for conveying the absorption liquid rich liquid and is suitable for driving the absorption liquid rich liquid to flow and adjusting the pressure of the absorption liquid rich liquid;
and the first pressure sensor is arranged in a pipeline between the first pump and the cathode chamber and is suitable for detecting the pressure of the absorption liquid rich liquid.
3. The CO according to claim 2 2 The integrated carbon negative device for capturing and electrolyzing is characterized in that,
the first input assembly further comprises:
a first valve arranged between the first pump and the CO 2 A pipeline between the absorption towers;
and the first buffer tank is arranged on a pipeline between the first valve and the first pump.
4. A CO according to claim 3 2 The integrated carbon negative device for capturing and electrolyzing is characterized in that,
the first output assembly comprises a first separator, a first mixer, a second pump and a second buffer tank which are sequentially connected, the first separator is connected with an output pipeline of the cathode chamber so as to split and output electrolysis reaction products of the cathode chamber and lean liquid of the absorption liquid, a bypass of the first mixer is connected with a second valve and a supplement liquid input pipeline controlled by the second valve, the first mixer is suitable for supplying the supplement liquid to supplement the lean liquid of the absorption liquid, the second pump is suitable for driving the lean liquid of the absorption liquid and the flow of the supplement liquid at the downstream of the first mixer, and the second buffer tank is provided with a first liquid level detection deviceThe first liquid level detection device is electrically connected with the second valve, and the output end of the second buffer tank is suitable for outputting the absorption liquid lean solution to the CO 2 An absorption tower; and/or
The first output assembly comprises a detection device which is suitable for detecting the logistics component of the electrolytic reaction product of the cathode chamber, and the detection device is connected with an output pipeline of the cathode chamber in a bypass way and is electrically connected with the first valve.
5. The CO of claim 4 2 The integrated carbon negative device for capturing and electrolyzing is characterized in that,
the second input assembly includes:
the third pump is arranged on the pipeline of the second input assembly for conveying the anolyte, and is suitable for driving the anolyte to flow and adjusting the pressure of the anolyte;
and the second pressure sensor is arranged on a pipeline between the third pump and the anode chamber and is suitable for detecting the pressure of the anolyte.
6. The CO of claim 5 2 The integrated carbon negative device for capturing and electrolyzing is characterized in that,
the second input assembly further comprises:
the third valve is arranged on an anode electrolyte input pipeline connected with the third pump;
the second mixer is arranged in a pipeline between the third pump and the third valve and is connected with the second output assembly to receive the electrolyte after reaction;
the third buffer tank is provided with a second liquid level detection device electrically connected with the third valve;
and the heater is arranged in a pipeline between the third pump and the anode chamber and is suitable for heating the temperature of the anolyte to be matched with the temperature of the liquid in the cathode chamber.
7. The CO of claim 6 2 Carbon negative device integrated with capturing electrolysisCharacterized in that,
the second output assembly comprises a second separator, the input end of the second separator is connected with an output pipeline of the anode chamber, one output end of the second separator is connected with the second mixer through a pipeline to return the electrolyte after reaction to the second input assembly, and the other output end of the second separator is suitable for outputting electrolytic reaction products of the anode chamber.
8. The CO according to claim 7 2 The integrated carbon negative device for capturing and electrolyzing is characterized in that,
the electrolytic cells are configured into a plurality of electrolytic reaction products of anode chambers which are distributed by a plurality of second separators in series, parallel or series-parallel connection, the electrolytic reaction products of the anode chambers which are distributed by the second separators are suitable for being output by the same third mixer, each second separator is suitable for outputting electrolyte after reaction to the anode chamber of the electrolytic cell at the downstream of the electrolytic cell, the anode chamber at the head end of a stroke is connected with a second input assembly, the second separator connected with the anode chamber at the tail end of the stroke is suitable for conveying the electrolyte after reaction back to the second mixer, the cathode chambers of the electrolytic cells are suitable for being connected, the cathode chamber at the head end of the stroke is connected with a first input assembly, and the electrolytic reaction products of the cathode chamber and the lean absorption liquid are distributed and output by the cathode chamber at the tail end of the stroke through the first separator.
9. A CO according to any one of claims 1 to 8 2 The integrated carbon negative device for capturing and electrolyzing is characterized in that,
the CO 2 The integrated carbon negative device for capturing and electrolyzing further comprises a shell body, wherein a containing space is formed in the shell body, the electrolysis module is arranged in the middle of the containing space, one side wall body of the shell body is provided with an anode electrolyte inlet, an absorbing liquid rich liquid inlet, an absorbing liquid lean liquid outlet and a supplementing liquid inlet, and the other opposite side wall body is provided with an anode chamber electrolysis reaction product outlet and a cathode chamber electrolysis reaction product outlet.
10. The CO according to claim 9 2 The integrated carbon negative device for capturing and electrolyzing is characterized in that,
and a tortuous and extended cathode chamber flow passage is formed in the cathode chamber for allowing the absorption liquid rich liquid to flow and react with the cathode catalyst, and a tortuous and extended anode chamber flow passage is formed in the anode chamber for allowing the anolyte to flow and react with the anode catalyst.
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