CN118345395A - Electrochemical method and device for realizing desorption and regeneration of carbon dioxide rich liquid - Google Patents
Electrochemical method and device for realizing desorption and regeneration of carbon dioxide rich liquid Download PDFInfo
- Publication number
- CN118345395A CN118345395A CN202410367639.7A CN202410367639A CN118345395A CN 118345395 A CN118345395 A CN 118345395A CN 202410367639 A CN202410367639 A CN 202410367639A CN 118345395 A CN118345395 A CN 118345395A
- Authority
- CN
- China
- Prior art keywords
- chamber
- liquid
- acidification
- gas
- cathode
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 186
- 239000007788 liquid Substances 0.000 title claims abstract description 168
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 94
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 45
- 230000008929 regeneration Effects 0.000 title claims abstract description 30
- 238000011069 regeneration method Methods 0.000 title claims abstract description 30
- 238000003795 desorption Methods 0.000 title claims abstract description 23
- 238000002848 electrochemical method Methods 0.000 title claims description 11
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 104
- 239000001257 hydrogen Substances 0.000 claims abstract description 104
- 230000020477 pH reduction Effects 0.000 claims abstract description 103
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 100
- 239000007789 gas Substances 0.000 claims abstract description 58
- 239000003792 electrolyte Substances 0.000 claims abstract description 24
- 239000003054 catalyst Substances 0.000 claims description 59
- 238000006243 chemical reaction Methods 0.000 claims description 37
- 229910000510 noble metal Inorganic materials 0.000 claims description 26
- 239000012528 membrane Substances 0.000 claims description 23
- 239000000203 mixture Substances 0.000 claims description 22
- 238000000034 method Methods 0.000 claims description 20
- 239000003014 ion exchange membrane Substances 0.000 claims description 19
- 230000008569 process Effects 0.000 claims description 16
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 13
- 238000010521 absorption reaction Methods 0.000 claims description 11
- 239000000047 product Substances 0.000 claims description 11
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims description 10
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 claims description 10
- 239000011810 insulating material Substances 0.000 claims description 10
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 claims description 10
- 238000007599 discharging Methods 0.000 claims description 8
- 238000012544 monitoring process Methods 0.000 claims description 7
- 238000009792 diffusion process Methods 0.000 claims description 6
- 238000005868 electrolysis reaction Methods 0.000 claims description 6
- 238000011049 filling Methods 0.000 claims description 6
- 239000010931 gold Substances 0.000 claims description 6
- 125000002887 hydroxy group Chemical group [H]O* 0.000 claims description 6
- 229910052751 metal Inorganic materials 0.000 claims description 6
- 239000002184 metal Substances 0.000 claims description 6
- 238000002156 mixing Methods 0.000 claims description 6
- 229910052755 nonmetal Inorganic materials 0.000 claims description 6
- 238000007254 oxidation reaction Methods 0.000 claims description 6
- 239000004417 polycarbonate Substances 0.000 claims description 6
- 229920006324 polyoxymethylene Polymers 0.000 claims description 6
- 238000006722 reduction reaction Methods 0.000 claims description 6
- 239000010948 rhodium Substances 0.000 claims description 6
- 229920006395 saturated elastomer Polymers 0.000 claims description 6
- 239000010936 titanium Substances 0.000 claims description 6
- 239000004734 Polyphenylene sulfide Substances 0.000 claims description 5
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 claims description 5
- 229920000122 acrylonitrile butadiene styrene Polymers 0.000 claims description 5
- 229910052799 carbon Inorganic materials 0.000 claims description 5
- 239000000463 material Substances 0.000 claims description 5
- 229920003229 poly(methyl methacrylate) Polymers 0.000 claims description 5
- 229920000728 polyester Polymers 0.000 claims description 5
- 239000004926 polymethyl methacrylate Substances 0.000 claims description 5
- -1 polyoxymethylene Polymers 0.000 claims description 5
- 229920000069 polyphenylene sulfide Polymers 0.000 claims description 5
- 229910052719 titanium Inorganic materials 0.000 claims description 5
- 229930040373 Paraformaldehyde Natural products 0.000 claims description 4
- 239000004952 Polyamide Substances 0.000 claims description 4
- KJTLSVCANCCWHF-UHFFFAOYSA-N Ruthenium Chemical compound [Ru] KJTLSVCANCCWHF-UHFFFAOYSA-N 0.000 claims description 4
- 229910021393 carbon nanotube Inorganic materials 0.000 claims description 4
- 239000002041 carbon nanotube Substances 0.000 claims description 4
- 239000010941 cobalt Substances 0.000 claims description 4
- 229910017052 cobalt Inorganic materials 0.000 claims description 4
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 claims description 4
- 230000001276 controlling effect Effects 0.000 claims description 4
- 150000004696 coordination complex Chemical class 0.000 claims description 4
- 230000000694 effects Effects 0.000 claims description 4
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 claims description 4
- 229910052737 gold Inorganic materials 0.000 claims description 4
- 229910021389 graphene Inorganic materials 0.000 claims description 4
- 229910052741 iridium Inorganic materials 0.000 claims description 4
- GKOZUEZYRPOHIO-UHFFFAOYSA-N iridium atom Chemical compound [Ir] GKOZUEZYRPOHIO-UHFFFAOYSA-N 0.000 claims description 4
- 239000012263 liquid product Substances 0.000 claims description 4
- 229910052759 nickel Inorganic materials 0.000 claims description 4
- 229910052763 palladium Inorganic materials 0.000 claims description 4
- 229910052697 platinum Inorganic materials 0.000 claims description 4
- 229920002647 polyamide Polymers 0.000 claims description 4
- 229920001230 polyarylate Polymers 0.000 claims description 4
- 229920000515 polycarbonate Polymers 0.000 claims description 4
- 229920013636 polyphenyl ether polymer Polymers 0.000 claims description 4
- 239000004800 polyvinyl chloride Substances 0.000 claims description 4
- 239000011347 resin Substances 0.000 claims description 4
- 229920005989 resin Polymers 0.000 claims description 4
- 229910052703 rhodium Inorganic materials 0.000 claims description 4
- MHOVAHRLVXNVSD-UHFFFAOYSA-N rhodium atom Chemical compound [Rh] MHOVAHRLVXNVSD-UHFFFAOYSA-N 0.000 claims description 4
- 229910052707 ruthenium Inorganic materials 0.000 claims description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 4
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 claims description 3
- BQCADISMDOOEFD-UHFFFAOYSA-N Silver Chemical compound [Ag] BQCADISMDOOEFD-UHFFFAOYSA-N 0.000 claims description 3
- 230000002378 acidificating effect Effects 0.000 claims description 3
- 239000007795 chemical reaction product Substances 0.000 claims description 3
- 239000012467 final product Substances 0.000 claims description 3
- 229910052750 molybdenum Inorganic materials 0.000 claims description 3
- 239000011733 molybdenum Substances 0.000 claims description 3
- 230000001590 oxidative effect Effects 0.000 claims description 3
- 229920000915 polyvinyl chloride Polymers 0.000 claims description 3
- 230000036647 reaction Effects 0.000 claims description 3
- 238000004064 recycling Methods 0.000 claims description 3
- 230000001105 regulatory effect Effects 0.000 claims description 3
- 229910052709 silver Inorganic materials 0.000 claims description 3
- 239000004332 silver Substances 0.000 claims description 3
- 230000002745 absorbent Effects 0.000 abstract description 10
- 239000002250 absorbent Substances 0.000 abstract description 10
- 230000008901 benefit Effects 0.000 abstract description 3
- 239000007864 aqueous solution Substances 0.000 abstract description 2
- 239000000243 solution Substances 0.000 description 10
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 description 6
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 5
- 150000002431 hydrogen Chemical class 0.000 description 5
- 238000010248 power generation Methods 0.000 description 5
- 239000010949 copper Substances 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 3
- 229910052802 copper Inorganic materials 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 239000006096 absorbing agent Substances 0.000 description 2
- 239000003513 alkali Substances 0.000 description 2
- 150000001412 amines Chemical class 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 150000002500 ions Chemical class 0.000 description 2
- 229910052742 iron Inorganic materials 0.000 description 2
- 230000014759 maintenance of location Effects 0.000 description 2
- 239000011572 manganese Substances 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 239000012994 photoredox catalyst Substances 0.000 description 2
- 229920003023 plastic Polymers 0.000 description 2
- 239000004033 plastic Substances 0.000 description 2
- HEMHJVSKTPXQMS-UHFFFAOYSA-M sodium hydroxide Inorganic materials [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 2
- 239000010935 stainless steel Substances 0.000 description 2
- 229910001220 stainless steel Inorganic materials 0.000 description 2
- 238000012546 transfer Methods 0.000 description 2
- HZAXFHJVJLSVMW-UHFFFAOYSA-N 2-Aminoethan-1-ol Chemical compound NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- PWHULOQIROXLJO-UHFFFAOYSA-N Manganese Chemical compound [Mn] PWHULOQIROXLJO-UHFFFAOYSA-N 0.000 description 1
- 239000004677 Nylon Substances 0.000 description 1
- 229930182556 Polyacetal Natural products 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- DHKHKXVYLBGOIT-UHFFFAOYSA-N acetaldehyde Diethyl Acetal Natural products CCOC(C)OCC DHKHKXVYLBGOIT-UHFFFAOYSA-N 0.000 description 1
- 125000002777 acetyl group Chemical class [H]C([H])([H])C(*)=O 0.000 description 1
- NIXOWILDQLNWCW-UHFFFAOYSA-N acrylic acid group Chemical group C(C=C)(=O)O NIXOWILDQLNWCW-UHFFFAOYSA-N 0.000 description 1
- XECAHXYUAAWDEL-UHFFFAOYSA-N acrylonitrile butadiene styrene Chemical compound C=CC=C.C=CC#N.C=CC1=CC=CC=C1 XECAHXYUAAWDEL-UHFFFAOYSA-N 0.000 description 1
- 239000004676 acrylonitrile butadiene styrene Substances 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 125000003118 aryl group Chemical group 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004880 explosion Methods 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 238000003837 high-temperature calcination Methods 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 229910052748 manganese Inorganic materials 0.000 description 1
- RCHKEJKUUXXBSM-UHFFFAOYSA-N n-benzyl-2-(3-formylindol-1-yl)acetamide Chemical compound C12=CC=CC=C2C(C=O)=CN1CC(=O)NCC1=CC=CC=C1 RCHKEJKUUXXBSM-UHFFFAOYSA-N 0.000 description 1
- 229920001778 nylon Polymers 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 230000009919 sequestration Effects 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- JBQYATWDVHIOAR-UHFFFAOYSA-N tellanylidenegermanium Chemical compound [Te]=[Ge] JBQYATWDVHIOAR-UHFFFAOYSA-N 0.000 description 1
Landscapes
- Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)
Abstract
The application discloses a device for realizing desorption and regeneration of carbon dioxide rich liquid, which comprises a three-chamber electrolytic cell, an acidification chamber accessory component, a cathode chamber accessory component, an electrolyte input component, an external hydrogen inlet and outlet component and power supply equipment, wherein the three-chamber electrolytic cell is connected with the acidification chamber accessory component; the three-chamber electrolytic cell comprises an anode chamber, an acidification chamber and a cathode chamber, wherein an inlet of the acidification chamber is connected with an electrolyte input assembly, an outlet of the acidification chamber and an inlet of the cathode chamber are connected with an acidification chamber auxiliary assembly, and an outlet of the cathode chamber is connected with a cathode chamber auxiliary assembly; the inlet of the anode chamber is provided with two inlets, the inlet of one anode chamber is connected with the cathode chamber accessory component, the inlet of the other anode chamber is connected with the air inlet part of the external hydrogen inlet and outlet component, the outlet of the anode chamber is connected with the air outlet part of the external hydrogen inlet and outlet component, and the power supply device is connected with the acidification chamber and the cathode chamber. Has the following advantages: the H2 generated by the cathode chamber can be utilized while CO2 in the absorbent aqueous solution is efficiently released, and no additional gas is generated by the anode chamber.
Description
Technical Field
The invention relates to the technical field of desorption and regeneration of carbon dioxide rich liquid, in particular to an electrochemical method and device for realizing desorption and regeneration of carbon dioxide rich liquid.
Background
Carbon dioxide (CO 2) is the most dominant greenhouse gas, and carbon dioxide emissions have increased year by year since the industrial revolution, and the climate change thereby brought about is attracting great attention worldwide. Carbon Capture and sequestration utilization (CCUS) technology, which is a powerful means of reducing CO2 emissions, refers to the removal of CO2 from the atmosphere by a variety of methods and its storage underground or utilization to reduce its impact on climate change, with the primary CO2 Capture technologies currently involving absorption and adsorption.
Absorption is a technique for treating and storing CO2 in air into a liquid using a chemical absorbent, and is widely used in industry. Wherein, the common absorbent such as organic amine compound monoethanolamine, inorganic alkali compound sodium hydroxide, potassium hydroxide and the like has good absorption efficiency, selectivity and reliability. These high efficiency absorbents are typically mixed with water to form an aqueous absorbent solution, relying on an absorber to achieve CO2 capture. In the absorber, the CO 2-containing gas (air, flue gas) is fully contacted with the aqueous absorbent solution at the packing layer and undergoes chemical reaction, and the CO2 is fixed into the aqueous absorbent solution to form a CO 2-rich liquid. The CO 2-rich liquid will then enter the corresponding desorption device releasing CO2.
However, the current resolution process has a number of common disadvantages, mainly in terms of energy consumption. Taking a monoalcohol amine process as an example, the CO2 analysis can be effectively performed only under the condition of 80-120 ℃; in the process represented by inorganic alkali absorbent such as potassium hydroxide, CO2 is obtained by a high-temperature calcination process, and the calcination temperature is generally 900 ℃ or higher. In addition, both of these typical processes require the construction of large-scale analytical equipment such as analytical towers, calcium hydroxide (Ca (OH) 2) precipitation process support facilities, calciners, etc., which are large in floor space and costly.
As a brand new technology in this field, this problem can be effectively solved by electrochemical methods. Electrochemical processes are usually carried out in electrolytic cells, the apparatus consisting of an anode compartment and a cathode compartment, with an ion exchange membrane sandwiched between them, by varying the pH of the anode and cathode compartments, effecting the release of CO2 and the regeneration of the aqueous absorbent solution.
The electrochemical method has the advantages of high efficiency, convenient start and stop and access to a regenerated power system. In addition, the method requires a smaller volume of release equipment, can be applied in a modularized manner, and is convenient to transport and install. However, current electrochemical methods also suffer from a number of disadvantages. For example, CO2 is released from the anode chamber with concomitant production of oxygen (O2), which makes the CO2 concentration low, requiring further purification; and additional hydrogen (H2) is generated in the cathode chamber. Meanwhile, the two additional gases are easy to cause explosion after being mixed, and the two additional gases belong to important potential safety hazards. This series of problems limits the industrial application of this technique.
Disclosure of Invention
The invention aims to solve the technical problems, and provides an electrochemical method and an electrochemical device for realizing desorption and regeneration of a carbon dioxide rich solution, which can efficiently release CO2 in an absorbent aqueous solution and simultaneously utilize H2 generated by a cathode chamber, and the anode chamber does not generate additional gas.
In order to solve the technical problems, the invention adopts the following technical scheme:
A device for realizing desorption and regeneration of carbon dioxide rich liquid comprises a three-chamber electrolytic cell, an acidification chamber accessory component, a cathode chamber accessory component, an electrolyte input component, an external hydrogen inlet and outlet component and power supply equipment;
The three-chamber electrolytic cell comprises an anode chamber, an acidification chamber and a cathode chamber, wherein the anode chamber is used for carrying out anodic oxidation reaction, the cathode chamber is used for carrying out cathodic reduction reaction, the acidification chamber is used for carrying out carbon dioxide release reaction, and in the acidification chamber, carbon dioxide absorption liquid releases carbon dioxide under an acidic condition; in the cathode chamber, the absorption liquid from the acidification chamber after reaction is regenerated, and the absorption liquid has carbon dioxide capturing capability again; the anode chamber only circulates hydrogen and does not circulate liquid;
an inlet of the acidification chamber is connected with the electrolyte input assembly, an outlet of the acidification chamber and an inlet of the cathode chamber are connected with the acidification chamber accessory assembly, and an outlet of the cathode chamber is connected with the cathode chamber accessory assembly; the inlet of the anode chamber is provided with two inlets, the inlet of one anode chamber is connected with the cathode chamber accessory component, the inlet of the other anode chamber is connected with the air inlet part of the external hydrogen inlet and outlet component, the outlet of the anode chamber is connected with the air outlet part of the external hydrogen inlet and outlet component, and the power supply device is connected with the acidification chamber and the cathode chamber.
Further, the acidification chamber is arranged between the cathode chamber and the anode chamber, a cathode chamber membrane electrode is arranged between the acidification chamber and the cathode chamber, the cathode chamber membrane electrode is used for reducing water to generate hydrogen and hydroxyl, an anode chamber membrane electrode is arranged between the acidification chamber and the anode chamber, and the anode chamber membrane electrode is used for oxidizing hydrogen to provide protons for the acidification chamber.
Further, the shell of the three-chamber electrolytic cell is made of an insulating material, and the insulating material is one or a mixture of two or more of polymethyl methacrylate, ABS plastic, polyvinyl chloride, transparent resin, polycarbonate, polyamide, polyoxymethylene, polyphenyl ether, polyester, polyphenylene sulfide and polyarylate.
Furthermore, the anode chamber, the acidification chamber and the cathode chamber are respectively provided with built-in flow channels, and the built-in flow channels are zigzag flow channels;
the built-in flow channels of the anode chamber and the cathode chamber are made of conductive metal;
the material of the built-in runner of the acidification chamber is an insulating material.
Further, the anode chamber membrane electrode comprises an ion exchange membrane, a catalyst layer is coated on the side surface of one side, close to the anode chamber, of the ion exchange membrane, and a gas diffusion layer is arranged on the catalyst layer;
The cathode chamber membrane electrode comprises an ion exchange membrane and a catalyst layer, wherein the catalyst layer is coated on the side surface of the ion exchange membrane, which is close to one side of the cathode chamber, and the ion exchange membrane and the catalyst layer are tightly combined.
Further, the catalyst layer is a noble metal-based catalyst, a non-noble metal-based catalyst, a mixture of two or more than two of the non-noble metal-based catalysts or a metal complex molecule composed of the noble metal-based catalyst and the non-noble metal-based catalyst;
The noble metal-based catalyst package is a mixture composed of one or more of platinum, palladium, ruthenium, iridium, rhodium, silver and gold; the non-noble metal-based catalyst is a mixture composed of one or more of nickel, cobalt, molybdenum and titanium; the nonmetal-based catalyst is a mixture composed of one or more of active carbon, graphene, carbon nano tube and derivatives thereof.
Further, the acidification chamber accessory assembly comprises an acidification gas-liquid buffer tank and a first pressure detector; the acidification gas-liquid buffer tank is connected with a gas discharge pipeline for conveying CO2, and a gas control valve is arranged on the gas discharge pipeline for regulating gas output;
The cathode chamber accessory assembly comprises a cathode gas-liquid buffer tank and a second pressure detector; the cathode gas-liquid buffer tank is connected with a regenerated liquid discharge pipeline, the regenerated liquid discharge pipeline is connected with a CO2 capturing module, and a second liquid control valve is arranged between the regenerated liquid discharge pipeline and the CO2 capturing module;
The external hydrogen inlet and outlet assembly comprises an external hydrogen input pipeline and a hydrogen output pipeline, the external hydrogen input pipeline is connected with the inlet of the anode chamber, and the hydrogen output pipeline is connected with the outlet of the anode chamber; the external hydrogen input pipeline is provided with a gas flowmeter and an air inlet valve which are respectively used for adjusting the external hydrogen input flow and controlling the external hydrogen input, and the hydrogen output pipeline is provided with an air outlet valve.
Further, the first pressure detector is a pressure sensor and is used for monitoring the pressure in the acidification gas-liquid buffer tank and the communicated acidification chamber, and the first pressure detector is arranged at the upper part of the acidification gas-liquid buffer tank;
The acidification gas-liquid buffer tank is connected with an outlet of the acidification chamber through a first gas-liquid mixing pipeline, the acidification gas-liquid buffer tank is connected with an inlet of the cathode chamber through a liquid outlet pipeline, and a first liquid control valve is arranged on the liquid outlet pipeline;
the first pressure detector is electrically connected with the gas control valve.
Further, the second pressure detector is a pressure sensor and is used for monitoring the pressure in the cathode gas-liquid buffer tank and the anode chamber; the second pressure detector is arranged at the top of the cathode gas-liquid buffer tank;
The cathode gas-liquid buffer tank is connected with the outlet of the cathode chamber through a second gas-liquid mixing pipeline; the cathode gas-liquid buffer tank is connected with one inlet of the anode chamber through a gas conveying pipeline.
An electrochemical method for realizing desorption and regeneration of carbon dioxide rich liquid comprises the following steps:
step1, conveying a trapping liquid saturated by carbon dioxide into an acidification chamber and a cathode chamber;
Step 2, discharging other gases of the anode chamber and the cathode gas-liquid buffer tank, and filling hydrogen;
step 2.1, opening an air inlet valve on an external hydrogen input pipeline to enable external hydrogen to be input into an anode chamber, filling hydrogen into the anode chamber, opening an air outlet valve on a hydrogen output pipeline, and discharging redundant hydrogen from an outlet connected with the hydrogen output pipeline; the process lasts for 1-10 minutes;
Step 2.2, a second liquid control valve between the cathode gas-liquid buffer tank and the CO2 capturing module is opened, an air outlet valve on a hydrogen output pipeline is closed, hydrogen enters the cathode gas-liquid buffer tank, other gases in the cathode gas-liquid buffer tank are discharged, and the process lasts for 1-10 minutes;
in the process of inputting hydrogen into the cathode gas-liquid buffer tank, a certain electrolyte is arranged in the cathode gas-liquid buffer tank, and the liquid level of the electrolyte part is beyond the outlet of the cathode gas-liquid buffer tank, so that the hydrogen is prevented from overflowing from the outlet;
Step 3, three-chamber electrolytic cell reaction
After the hydrogen is filled, closing a second liquid control valve between the cathode gas-liquid buffer tank and the CO2 capturing module and an air inlet valve on an external hydrogen input pipeline; starting a power supply, starting an electrolytic reaction, and opening a valve on an electrolyte input assembly after 1-3 minutes of electrolysis to recover electrolyte supply;
Step 3.1 Anode Chamber reaction
The anode chamber is subjected to oxidation reaction, and H2 is oxidized to generate protons;
The reaction formula is as follows:
H2-2e-→2H+；
step 3.2 acidification chamber reaction
Protons in the anode chamber enter the acidification chamber through the anode membrane electrode to react with the trapping liquid saturated by carbon dioxide, a gas product is carbon dioxide, and a liquid product is the trapping liquid after releasing CO 2;
The reaction product of the acidification chamber flows into the acidification gas-liquid buffer tank, when the pressure in the acidification gas-liquid buffer tank is more than or equal to 130kPa, a gas control valve on a gas discharge pipeline is opened, CO2 is output and collected, when the pressure is smaller than the value, the gas control valve is closed and waits for the pressure to rise, and the trapping liquid after releasing CO2 enters a cathode chamber for regeneration.
Detecting the components of the gas product every 20 minutes after the reaction starts, and gradually improving the purity of CO2 along with the progress of the reaction, wherein the purity of the final product CO2 is more than or equal to 98 percent.
Step 3.3 cathode Chamber reaction
Hydrogen is transferred to the anode chamber to be oxidized again, so that the recycling of the hydrogen is realized; the hydroxyl and the lean solution are combined and reacted to realize regeneration, so as to obtain a regenerated trapping solution with trapping capacity;
the H2 and the regenerated trapping liquid flow into the cathode gas-liquid buffer tank along with the pipeline, and when the pressure in the cathode gas-liquid buffer tank is more than or equal to 130kPa, the hydrogen is conveyed to the anode chamber under the pressure effect;
The reduction reaction formula is as follows:
4H2O+4e-→4OH-+2H2。
Compared with the prior art, the invention has the following technical effects:
1. Solves the problem of hydrogen production by the cathode in the conventional CO2 release technology by electrolysis, ensures that the hydrogen is utilized at the anode, and effectively reduces the potential safety hazard in the production process.
2. The problem of oxygen production by the anode is avoided, the purity of CO2 can be greatly improved, and the purity of CO2 is more than or equal to 98 percent.
3. The energy consumption is low, the CO2 release efficiency is high, and the CO2 release efficiency is more than or equal to 95%;
4. the required single electrolysis equipment is small in size, the stack body can be formed in a modularized combination mode, the transportation and the installation are convenient, and the occupied area is controllable.
5. Clean energy sources such as wind power generation, photovoltaic power generation, tidal power generation and the like can be utilized, and the energy-saving device has good economic benefits.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below. Like elements or portions are generally identified by like reference numerals throughout the several figures. In the drawings, elements or portions thereof are not necessarily drawn to scale.
Fig. 1 is a schematic structural diagram of a device for desorption and regeneration of a carbon dioxide rich liquid in the invention.
Detailed Description
An embodiment is shown in fig. 1, and the device for realizing desorption regeneration of carbon dioxide rich liquid comprises a three-chamber electrolytic cell, an acidification chamber accessory component, a cathode chamber accessory component, an electrolyte input component, an external hydrogen inlet and outlet component and power equipment.
The three-chamber electrolytic cell comprises an anode chamber 12, an acidification chamber 14 and a cathode chamber 16, wherein the anode chamber 12 is used for carrying out anodic oxidation reaction, the cathode chamber 16 is used for carrying out cathodic reduction reaction, the acidification chamber 14 is used for carrying out carbon dioxide release reaction, and in the acidification chamber, carbon dioxide absorption liquid releases carbon dioxide under acidic conditions; in the cathode chamber, the absorption liquid from the acidification chamber after reaction is regenerated, and the absorption liquid has carbon dioxide capturing capability again; the anode chamber only circulates hydrogen and does not circulate liquid. The acidification chamber 14 is arranged between the cathode chamber 16 and the anode chamber 12, a cathode chamber membrane electrode 15 is arranged between the acidification chamber 14 and the cathode chamber 16, the cathode chamber membrane electrode 15 is used for reducing water to generate hydrogen and hydroxyl, an anode chamber membrane electrode 13 is arranged between the acidification chamber 14 and the anode chamber 12, the anode chamber membrane electrode 13 is used for oxidizing hydrogen, and protons are provided for the acidification chamber 14.
An inlet of the acidification chamber 14 is connected with an electrolyte input assembly, an outlet of the acidification chamber 14 and an inlet of the cathode chamber 16 are connected with an acidification chamber auxiliary assembly, and an outlet of the cathode chamber 16 is connected with a cathode chamber auxiliary assembly; the inlets of the anode chambers 12 are arranged in two, the inlet of one anode chamber 12 is connected with the cathode chamber auxiliary assembly, the inlet of the other anode chamber 12 is connected with the air inlet part of the external hydrogen inlet and outlet assembly, and the outlet of the anode chamber 12 is connected with the air outlet part of the external hydrogen inlet and outlet assembly.
The shell of the three-chamber electrolytic cell adopts an insulating material, and the insulating material is one or a mixture of two or more of polymethyl methacrylate (PMMA, acrylic), ABS plastic (acrylonitrile-butadiene-styrene), polyvinyl chloride (PVC), transparent resin, polycarbonate (PC, PC plastic), polyamide (PA, nylon), polyoxymethylene (POM, acetal, polyacetal, aldehyde resin, sai steel, terling), polyphenyl ether (MPPO, PPO plastic), polyester, polyphenylene sulfide (PPS) and polyarylate (aromatic polyester, PAR for short).
The anode chamber 12, the acidification chamber 14 and the cathode chamber 16 are respectively provided with built-in flow channels, the built-in flow channels are zigzag flow channels, and are provided with various zigzag shapes, and each flow channel is any one of single-line snakelike, multi-line snakelike, square spiral, parallel straight line alternate and grid, so that the contact between liquid and a catalyst can be increased, and the reaction is promoted.
The material of the built-in runner of the anode chamber 12 is conductive metal, and the conductive metal is one or a mixture of two or more of titanium, stainless steel, iron and copper.
The material of the built-in flow channel of the cathode chamber 16 is conductive metal, and the conductive metal is one or a mixture of two or more of titanium, stainless steel, iron and copper.
The material of the built-in runner of the acidification chamber 16 is an insulating material, and the insulating material is one or a mixture of two or more of polymethyl methacrylate, ABS plastic, polyvinyl chloride, transparent resin, polycarbonate, polyamide, polyoxymethylene, polyphenyl ether, polyester, polyphenylene sulfide and polyarylate.
The anode chamber membrane electrode 13 comprises an ion exchange membrane, a catalyst layer is coated on the side surface of the ion exchange membrane, which is close to one side of the anode chamber, a gas diffusion layer is arranged on the catalyst layer, the catalyst layer is coated on the ion exchange membrane and is tightly attached to the gas diffusion layer, the ion exchange membrane is used for providing ion transfer, a catalyst on the catalyst layer promotes reaction, the gas diffusion layer plays a role in diffusing hydrogen, the hydrogen directly reacts unevenly on the catalyst layer, and the gas and the catalyst are required to be fully contacted and reacted through the gas diffusion layer.
The catalyst layer of the anode chamber membrane electrode 13 is a noble metal-based catalyst, a non-noble metal-based catalyst, a mixture of two or more non-metal-based catalysts or a metal complex molecule composed of the noble metal-based catalyst and the non-noble metal-based catalyst; the noble metal-based catalyst is one or a mixture of more of platinum (Pt), palladium (Pd), ruthenium (Ru), iridium (Ir), rhodium (Rh) and gold (Au); the non-noble metal-based catalyst is a mixture composed of one or more of manganese (Mn), iron (Fe), cobalt (Co), nickel (Ni), copper (Cu) and zinc (Zn); the nonmetal-based catalyst is a mixture composed of one or more of active carbon, graphene, carbon nano tube and derivatives thereof.
The cathode chamber membrane electrode 15 comprises an ion exchange membrane and a catalyst layer, wherein the catalyst layer is coated on the side surface of the ion exchange membrane, which is close to one side of the cathode chamber 16, the ion exchange membrane is used for providing ion transfer, and the catalyst on the catalyst layer promotes reaction to occur, and the ion exchange membrane and the catalyst layer are tightly combined.
The catalyst layer of the cathode membrane electrode 15 is a noble metal-based catalyst, a non-noble metal catalyst, a mixture of two or more non-metal-based catalysts or a metal complex molecule composed of a noble metal-based catalyst and a non-noble metal-based catalyst; the noble metal-based catalyst package is a mixture composed of one or more of platinum (Pt), palladium (Pd), ruthenium (Ru), iridium (Ir), rhodium (Rh), silver (Ag) and gold (Au); the non-noble metal-based catalyst is a mixture composed of one or more of nickel (Ni), cobalt (Co), molybdenum (Mo) and titanium (Ti); the nonmetal-based catalyst is a mixture composed of one or more of active carbon, graphene, carbon nano tube and derivatives thereof.
The acidification chamber sub-assembly separates the acidification chamber 14 effluent product and allows the gaseous product output, the liquid product to flow further into the cathode chamber 16 and fill it; the acidification chamber sub-assembly comprises an acidification gas-liquid buffer tank 17 and a first pressure detector 18; the acidification gas-liquid buffer tank 17 is used for separating the outflow product in the acidification chamber; the first pressure detector 18 is a pressure sensor for monitoring the pressure in the acidification gas-liquid buffer tank and the communication acidification chamber, and the first pressure detector 18 is arranged at the upper part of the acidification gas-liquid buffer tank 17.
The acidification gas-liquid buffer tank 17 is connected with the outlet of the acidification chamber 14 through a first gas-liquid mixing pipeline 31, the acidification gas-liquid buffer tank 17 is connected with the inlet of the cathode chamber 16 through a liquid outlet pipeline 32, and a first liquid control valve 20 is arranged on the liquid outlet pipeline 32.
The acidification gas-liquid buffer tank 17 is also connected with a gas discharge pipeline 33 for delivering CO2, and the gas discharge pipeline 33 is provided with a gas control valve 19 for regulating gas output.
The first pressure detector 18 is in circuit connection with the gas control valve 19 and is used for monitoring and adjusting the pressure in the acidification gas-liquid buffer tank in real time and controlling the output flow of a gas product; when the pressure in the acidification gas-liquid buffer tank is more than or equal to 130kPa, the gas control valve is opened to start delivering CO2, and when the pressure is less than the value, the gas control valve is closed to wait for the pressure to rise.
The cathode chamber auxiliary assembly is used for inputting hydrogen into the anode chamber and discharging regenerated liquid into the C02 capture module, the cathode chamber auxiliary assembly comprises a cathode gas-liquid buffer tank 21 and a second pressure detector 22, and the cathode gas-liquid buffer tank 21 is used for separating effluent products of the cathode chamber 16; the second pressure detector 22 is a pressure sensor and is used for monitoring the pressure in the cathode gas-liquid buffer tank 21 and the communicated anode chamber 12; the second pressure detector 22 is provided on the top of the cathode gas-liquid buffer tank 21.
The cathode gas-liquid buffer tank 21 is connected with the outlet of the cathode chamber 16 through a second gas-liquid mixing pipeline 34; the cathode gas-liquid buffer tank 21 is connected with one inlet of the anode chamber 12 through a gas conveying pipeline 35; the cathode gas-liquid buffer tank 21 is connected with a regenerated liquid discharge pipeline 36, the regenerated liquid discharge pipeline 36 is connected with a CO2 capturing module, and a second liquid control valve 24 is arranged between the regenerated liquid discharge pipeline 36 and the regenerated liquid discharge pipeline 36.
The electrolyte input assembly includes an electrolyte input line 37, the electrolyte input line 37 connecting the inlet of the acidification chamber 14 and the CO2 capture module.
The external hydrogen inlet and outlet assembly includes an external hydrogen inlet conduit 39 and a hydrogen outlet conduit 38; an external hydrogen input pipe 39 is connected to the inlet of the anode chamber 12, and a hydrogen output pipe 38 is connected to the outlet of the anode chamber 12; the external hydrogen input pipeline 39 is provided with a gas flow meter and an air inlet valve 26, which are respectively used for adjusting the external hydrogen input flow and controlling the external hydrogen input, and the hydrogen output pipeline 38 is provided with an air outlet valve 23.
Before the three-chamber electrolytic cell starts the electrolytic reaction to release CO2, the external hydrogen inlet and outlet assembly inputs hydrogen and discharges other gases in the anode chamber so as to be full of hydrogen.
The power supply device comprises a power converter and a power system; the power converter is used for converting alternating current into direct current, and the power system comprises wind power, photovoltaic power generation, tidal power generation, nuclear power and conventional power utilization; the power converter is connected to the power system, and the power converter is connected to the cathode chamber 16 and the anode chamber 12.
An electrochemical method for realizing desorption and regeneration of carbon dioxide rich liquid comprises the following steps:
step1, conveying a trapping liquid saturated by carbon dioxide into an acidification chamber and a cathode chamber;
Step 2, discharging other gases of the anode chamber and the cathode gas-liquid buffer tank, and filling hydrogen;
Step 2.1, opening an air inlet valve on an external hydrogen input pipeline to enable external hydrogen to be input into an anode chamber, filling hydrogen into the anode chamber, opening a valve on a hydrogen output pipeline of the anode chamber, and discharging redundant hydrogen from an outlet connected with the valve; the process lasts for 1-10 minutes.
And 2.2, opening a second liquid control valve between the cathode gas-liquid buffer tank and the CO2 capturing module, closing an air outlet valve on the hydrogen output pipeline, allowing hydrogen to enter the cathode gas-liquid buffer tank, and discharging other gases in the cathode gas-liquid buffer tank, wherein the process lasts for 1-10 minutes.
In the process of inputting hydrogen into the cathode gas-liquid buffer tank, a certain electrolyte is arranged in the cathode gas-liquid buffer tank, and the liquid level of the electrolyte part is beyond the outlet of the cathode gas-liquid buffer tank, so that the hydrogen is prevented from overflowing from the outlet.
Step 3, three-chamber electrolytic cell reaction
After the hydrogen is filled, closing a second liquid control valve between the cathode gas-liquid buffer tank and the CO2 capturing module and an air inlet valve on an external hydrogen input pipeline; and (3) starting a power supply, starting an electrolytic reaction, and opening a valve on an electrolyte input pipeline after electrolysis for 1-3 minutes to recover electrolyte supply.
Step 3.1 Anode Chamber reaction
The anode chamber is subjected to oxidation reaction, and H2 is oxidized to generate protons;
The reaction formula is as follows:
H2-2e-→2H+；
Step 3.2 acidification chamber reaction (CO 2 release)
Protons in the anode chamber enter the acidification chamber through the anode membrane electrode to react with the trapping liquid (rich liquid) saturated by carbon dioxide, the gas product is carbon dioxide, and the liquid product is the trapping liquid (lean liquid) after releasing CO 2.
The reaction product of the acidification chamber flows into the acidification gas-liquid buffer tank, when the pressure in the acidification gas-liquid buffer tank is more than or equal to 130kPa, a gas control valve on a gas discharge pipeline is opened, CO2 is output and collected, and when the pressure is less than the value, the gas control valve is closed and waits for the pressure to rise, and lean liquid enters a cathode chamber for regeneration.
Detecting the components of the gas product every 20 minutes after the reaction starts, and gradually improving the purity of CO2 along with the progress of the reaction, wherein the purity of the final product CO2 is more than or equal to 98 percent.
Step 3.3 cathode Chamber reaction (trapped liquid regeneration)
Hydrogen is transferred to the anode chamber to be oxidized again, so that the recycling of the hydrogen is realized; the hydroxyl and the lean solution are combined and reacted to realize regeneration, so as to obtain a regenerated trapping solution with trapping capacity;
the H2 and the regenerated trapping liquid flow into the cathode gas-liquid buffer tank together along with the pipeline, and when the pressure in the cathode gas-liquid buffer tank is more than or equal to 130kPa, the hydrogen is conveyed to the anode chamber under the pressure effect.
The reduction reaction formula is as follows:
4H2O+4e-→4OH-+2H2。
The electrolytic reaction parameters were as follows: the electrolytic reaction is carried out at room temperature; the current density is 100-2000 mA/cm2, and the cell pressure (electrolytic voltage) is 0.3-30.0V; the hydraulic retention time of the electrolyte is 1-30 min.
Preferably, at a current density of 125mA/cm2, the electrolysis voltage is about 5.0V, the hydraulic retention time is 2min, at which value CO2 is almost 100% released, and the energy consumption is low.
The description of the present invention has been presented for purposes of illustration and description, and is not intended to be exhaustive or limited to the invention in the form disclosed. Many modifications and variations will be apparent to those of ordinary skill in the art. The embodiments were chosen and described in order to best explain the principles of the invention and the practical application, and to enable others of ordinary skill in the art to understand the invention for various embodiments with various modifications as are suited to the particular use contemplated.
Claims (10)
1. The device for realizing desorption and regeneration of the carbon dioxide rich liquid is characterized in that: comprises a three-chamber electrolytic cell, an acidification chamber accessory component, a cathode chamber accessory component, an electrolyte input component, an external hydrogen inlet and outlet component and a power supply device;
The three-chamber electrolytic cell comprises an anode chamber (12), an acidification chamber (14) and a cathode chamber (16), wherein the anode chamber (12) is used for performing anodic oxidation reaction, the cathode chamber (16) is used for performing cathodic reduction reaction, the acidification chamber (14) is used for performing carbon dioxide release reaction, and in the acidification chamber (14), carbon dioxide absorption liquid releases carbon dioxide under an acidic condition; in the cathode chamber (16), the absorption liquid from the acidification chamber (14) after reaction is regenerated, and the carbon dioxide capturing capacity is provided again; the anode chamber (12) only circulates hydrogen and does not circulate liquid;
An inlet of the acidification chamber (14) is connected with an electrolyte input assembly, an outlet of the acidification chamber (14) and an inlet of the cathode chamber (16) are connected with an acidification chamber auxiliary assembly, and an outlet of the cathode chamber (16) is connected with a cathode chamber auxiliary assembly; the inlets of the anode chambers (12) are provided with two, wherein the inlet of one anode chamber (12) is connected with the cathode chamber auxiliary assembly, the inlet of the other anode chamber (12) is connected with the air inlet part of the external hydrogen inlet and outlet assembly, the outlet of the anode chamber (12) is connected with the air outlet part of the external hydrogen inlet and outlet assembly, and the power supply equipment is connected with the acidification chamber (14) and the cathode chamber (16).
2. The apparatus for realizing desorption regeneration of carbon dioxide rich liquid according to claim 1, wherein: the acidification chamber (14) is arranged between the cathode chamber (16) and the anode chamber (12), a cathode chamber membrane electrode (15) is arranged between the acidification chamber (14) and the cathode chamber (16), the cathode chamber membrane electrode (15) acts as reducing water to generate hydrogen and hydroxyl, an anode chamber membrane electrode (13) is arranged between the acidification chamber (14) and the anode chamber (12), and the anode chamber membrane electrode (13) acts as oxidizing hydrogen to provide protons for the acidification chamber (14).
3. The apparatus for realizing desorption regeneration of carbon dioxide rich liquid according to claim 1, wherein: the shell of the three-chamber electrolytic cell is made of an insulating material, and the insulating material is one or a mixture of two or more of polymethyl methacrylate, ABS plastic, polyvinyl chloride, transparent resin, polycarbonate, polyamide, polyoxymethylene, polyphenyl ether, polyester, polyphenylene sulfide and polyarylate.
4. The apparatus for realizing desorption regeneration of carbon dioxide rich liquid according to claim1, wherein: the anode chamber (12), the acidification chamber (14) and the cathode chamber (16) are respectively provided with built-in flow passages which are zigzag flow passages;
the built-in flow channels of the anode chamber (12) and the cathode chamber (16) are made of conductive metal;
the material of the built-in runner of the acidification chamber (14) is an insulating material.
5. A device for effecting desorption regeneration of a carbon dioxide rich liquid as claimed in claim 2, wherein: the anode chamber membrane electrode (13) comprises an ion exchange membrane, a catalyst layer is coated on the side surface of one side, close to the anode chamber, of the ion exchange membrane, and a gas diffusion layer is arranged on the catalyst layer;
The cathode chamber membrane electrode (15) comprises an ion exchange membrane and a catalyst layer, wherein the catalyst layer is coated on the side surface of one side, close to the cathode chamber (16), of the ion exchange membrane, and the ion exchange membrane and the catalyst layer are tightly combined.
6. The apparatus for realizing desorption regeneration of carbon dioxide rich liquid according to claim 5, wherein: the catalyst layer is a noble metal-based catalyst, a non-noble metal-based catalyst, a mixture of two or more than two of the non-noble metal-based catalysts or a metal complex molecule composed of the noble metal-based catalyst and the non-noble metal-based catalyst;
The noble metal-based catalyst package is a mixture composed of one or more of platinum, palladium, ruthenium, iridium, rhodium, silver and gold; the non-noble metal-based catalyst is a mixture composed of one or more of nickel, cobalt, molybdenum and titanium; the nonmetal-based catalyst is a mixture composed of one or more of active carbon, graphene, carbon nano tube and derivatives thereof.
7. The apparatus for realizing desorption regeneration of carbon dioxide rich liquid according to claim 1, wherein: the acidification chamber accessory assembly comprises an acidification gas-liquid buffer tank (17) and a first pressure detector (18); the acidification gas-liquid buffer tank (17) is connected with a gas discharge pipeline (33) for conveying CO2, and the gas discharge pipeline (33) is provided with a gas control valve (19) for regulating gas output;
The cathode chamber sub-assembly comprises a cathode gas-liquid buffer tank (21) and a second pressure detector (22); the cathode gas-liquid buffer tank (21) is connected with a regenerated liquid discharge pipeline (36), the regenerated liquid discharge pipeline (36) is connected with a CO2 capturing module, and a second liquid control valve (24) is arranged between the regenerated liquid discharge pipeline (36) and the CO2 capturing module;
The external hydrogen inlet and outlet assembly comprises an external hydrogen input pipeline (39) and a hydrogen output pipeline (38), wherein the external hydrogen input pipeline (39) is connected with the inlet of the anode chamber (12), and the hydrogen output pipeline (38) is connected with the outlet of the anode chamber (12); the external hydrogen input pipeline (39) is provided with a gas flowmeter and an air inlet valve (26) which are respectively used for adjusting the external hydrogen input flow and controlling the external hydrogen input, and the hydrogen output pipeline (38) is provided with an air outlet valve (23).
8. The apparatus for effecting desorption regeneration of a carbon dioxide rich liquid as defined in claim 7, wherein: the first pressure detector (18) is a pressure sensor and is used for monitoring the pressure in the acidification gas-liquid buffer tank and the communicated acidification chamber, and the first pressure detector (18) is arranged at the upper part of the acidification gas-liquid buffer tank (17);
The acidification gas-liquid buffer tank (17) is connected with an outlet of the acidification chamber (14) through a first gas-liquid mixing pipeline (31), the acidification gas-liquid buffer tank (17) is connected with an inlet of the cathode chamber (16) through a liquid outlet pipeline (32), and a first liquid control valve (20) is arranged on the liquid outlet pipeline (32);
The first pressure detector (18) is electrically connected to a gas control valve (19).
9. The apparatus for effecting desorption regeneration of a carbon dioxide rich liquid as defined in claim 7, wherein: the second pressure detector (22) is a pressure sensor and is used for monitoring the pressure in the cathode gas-liquid buffer tank (21) and the communicated anode chamber (12); the second pressure detector (22) is arranged at the top of the cathode gas-liquid buffer tank (21);
The cathode gas-liquid buffer tank (21) is connected with the outlet of the cathode chamber (16) through a second gas-liquid mixing pipeline (34); the cathode gas-liquid buffer tank (21) is connected with one inlet of the anode chamber (12) through a gas conveying pipeline (35).
10. An electrochemical method for realizing desorption and regeneration of carbon dioxide rich liquid is characterized in that: the electrochemical method is realized based on the device for realizing desorption and regeneration of the carbon dioxide rich liquid according to claim 7, and comprises the following steps:
step1, conveying a trapping liquid saturated by carbon dioxide into an acidification chamber and a cathode chamber;
Step 2, discharging other gases of the anode chamber and the cathode gas-liquid buffer tank, and filling hydrogen;
step 2.1, opening an air inlet valve on an external hydrogen input pipeline to enable external hydrogen to be input into an anode chamber, filling hydrogen into the anode chamber, opening an air outlet valve on a hydrogen output pipeline, and discharging redundant hydrogen from an outlet connected with the hydrogen output pipeline; the process lasts for 1-10 minutes;
Step 2.2, a second liquid control valve between the cathode gas-liquid buffer tank and the CO2 capturing module is opened, an air outlet valve on a hydrogen output pipeline is closed, hydrogen enters the cathode gas-liquid buffer tank, other gases in the cathode gas-liquid buffer tank are discharged, and the process lasts for 1-10 minutes;
in the process of inputting hydrogen into the cathode gas-liquid buffer tank, a certain electrolyte is arranged in the cathode gas-liquid buffer tank, and the liquid level of the electrolyte part is beyond the outlet of the cathode gas-liquid buffer tank, so that the hydrogen is prevented from overflowing from the outlet;
Step 3, three-chamber electrolytic cell reaction
After the hydrogen is filled, closing a second liquid control valve between the cathode gas-liquid buffer tank and the CO2 capturing module and an air inlet valve on an external hydrogen input pipeline; starting a power supply, starting an electrolytic reaction, and opening a valve on an electrolyte input assembly after 1-3 minutes of electrolysis to recover electrolyte supply;
Step 3.1 Anode Chamber reaction
The anode chamber is subjected to oxidation reaction, and H2 is oxidized to generate protons;
The reaction formula is as follows:
H2-2e-→2H+；
step 3.2 acidification chamber reaction
Protons in the anode chamber enter the acidification chamber through the anode membrane electrode to react with the trapping liquid saturated by carbon dioxide, a gas product is carbon dioxide, and a liquid product is the trapping liquid after releasing CO 2;
The reaction product of the acidification chamber flows into the acidification gas-liquid buffer tank, when the pressure in the acidification gas-liquid buffer tank is more than or equal to 130kPa, a gas control valve on a gas discharge pipeline is opened, CO2 is output and collected, when the pressure is smaller than the value, the gas control valve is closed and waits for the pressure to rise, and the trapping liquid after releasing CO2 enters a cathode chamber for regeneration.
Detecting the components of the gas product every 20 minutes after the reaction starts, and gradually improving the purity of CO2 along with the progress of the reaction, wherein the purity of the final product CO2 is more than or equal to 98%;
Step 3.3 cathode Chamber reaction
Hydrogen is transferred to the anode chamber to be oxidized again, so that the recycling of the hydrogen is realized; the hydroxyl and the lean solution are combined and reacted to realize regeneration, so as to obtain a regenerated trapping solution with trapping capacity;
the H2 and the regenerated trapping liquid flow into the cathode gas-liquid buffer tank along with the pipeline, and when the pressure in the cathode gas-liquid buffer tank is more than or equal to 130kPa, the hydrogen is conveyed to the anode chamber under the pressure effect;
The reduction reaction formula is as follows:
4H2O+4e-→4OH-+2H2。
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202410367639.7A CN118345395A (en) | 2024-03-28 | 2024-03-28 | Electrochemical method and device for realizing desorption and regeneration of carbon dioxide rich liquid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202410367639.7A CN118345395A (en) | 2024-03-28 | 2024-03-28 | Electrochemical method and device for realizing desorption and regeneration of carbon dioxide rich liquid |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN118345395A true CN118345395A (en) | 2024-07-16 |
Family
ID=91816257
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202410367639.7A Pending CN118345395A (en) | 2024-03-28 | 2024-03-28 | Electrochemical method and device for realizing desorption and regeneration of carbon dioxide rich liquid |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN118345395A (en) |
-
2024
- 2024-03-28 CN CN202410367639.7A patent/CN118345395A/en active Pending
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US11207643B2 (en) | Energy efficient removal of CO2 from air by integrating with H2 generation | |
| JP7297710B2 (en) | carbon dioxide reactor | |
| KR20170021713A (en) | Functional electrolysis cell for capturing and collecting NOx using FeEDTA | |
| CN111549355A (en) | Low cost CO electrolysis in solid oxide electrolytic cell2System and method for preparing synthesis gas | |
| CN115044921B (en) | Carbon dioxide treatment device, carbon dioxide treatment method, and carbide production method | |
| KR20200095953A (en) | Electrochemical system for producing ammonium nitrate from nitrogen oxides and preparation method thereof | |
| CN118345395A (en) | Electrochemical method and device for realizing desorption and regeneration of carbon dioxide rich liquid | |
| CN115646138B (en) | System for capturing carbon dioxide by solar-assisted electrochemical method | |
| US9263756B1 (en) | Electrochemical method for the removal of PPM levels of carbon monoxide from hydrogen for a fuel cell | |
| WO2023178913A1 (en) | Hydrogen impurity purification apparatus used for fuel cell | |
| JP7282725B2 (en) | Chemical reaction system, chemical reaction method, and valuables production system | |
| CN115125545A (en) | Carbon dioxide treatment device and method for producing carbon compound | |
| JP7490006B2 (en) | Carbon dioxide treatment device, carbon dioxide treatment method, and carbon compound production method | |
| CN114807997B (en) | Cathode for electrocatalytic reduction of carbon dioxide, electrolytic cell device and method | |
| JP7478769B2 (en) | Carbon dioxide treatment device, carbon dioxide treatment method, and ethylene production method | |
| AU2022221423B2 (en) | Electrolytic device and method of driving electrolytic device | |
| CN118727008A (en) | Carbon dioxide treatment device and carbon dioxide treatment method | |
| TWI795890B (en) | How to make ethylene oxide | |
| CN118437134A (en) | Direct capture of CO in air using a cooling tower2Method and apparatus of (a) | |
| CN118727015A (en) | Carbon dioxide treatment device, carbon dioxide treatment method, and ethylene production method | |
| Samiee et al. | Role of Hydrogen in Polymer Electrolyte Fuel Cell Systems | |
| Mohammadpour et al. | Electrolytic Regeneration of Spent Caustic Soda from CO2 Capture Systems | |
| CN117448842A (en) | Method and device for producing hydrogen by carbon trapping coupling | |
| CN117248228A (en) | Coupling integrated system for capturing and converting carbon dioxide | |
| CN118045471A (en) | Carbon capturing and synchronous fuel synthesizing device and method for lean carbon source |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |