CN115198289A - Electrocatalytic reduction of CO by electrode coating method of intermittent electrolyte 2 Reaction method - Google Patents
Electrocatalytic reduction of CO by electrode coating method of intermittent electrolyte 2 Reaction method Download PDFInfo
- Publication number
- CN115198289A CN115198289A CN202210586106.9A CN202210586106A CN115198289A CN 115198289 A CN115198289 A CN 115198289A CN 202210586106 A CN202210586106 A CN 202210586106A CN 115198289 A CN115198289 A CN 115198289A
- Authority
- CN
- China
- Prior art keywords
- cathode
- reactor
- electrolyte
- reaction
- cathode reactor
- 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.)
- Granted
Links
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B3/00—Electrolytic production of organic compounds
- C25B3/01—Products
- C25B3/03—Acyclic or carbocyclic hydrocarbons
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B11/00—Electrodes; Manufacture thereof not otherwise provided for
- C25B11/02—Electrodes; Manufacture thereof not otherwise provided for characterised by shape or form
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B15/00—Operating or servicing cells
- C25B15/02—Process control or regulation
- C25B15/021—Process control or regulation of heating or cooling
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B15/00—Operating or servicing cells
- C25B15/02—Process control or regulation
- C25B15/023—Measuring, analysing or testing during electrolytic production
- C25B15/025—Measuring, analysing or testing during electrolytic production of electrolyte parameters
- C25B15/027—Temperature
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B15/00—Operating or servicing cells
- C25B15/08—Supplying or removing reactants or electrolytes; Regeneration of electrolytes
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B3/00—Electrolytic production of organic compounds
- C25B3/01—Products
- C25B3/07—Oxygen containing compounds
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B3/00—Electrolytic production of organic compounds
- C25B3/20—Processes
- C25B3/25—Reduction
- C25B3/26—Reduction of carbon dioxide
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B9/00—Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
- C25B9/17—Cells comprising dimensionally-stable non-movable electrodes; Assemblies of constructional parts thereof
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/133—Renewable energy sources, e.g. sunlight
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Electrochemistry (AREA)
- Materials Engineering (AREA)
- Metallurgy (AREA)
- Automation & Control Theory (AREA)
- Analytical Chemistry (AREA)
- Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)
Abstract
The invention discloses an electrode coating method for intermittent electrolyte to electrocatalytically reduce CO 2 The reaction method can intermittently spray liquid electrolyte membrane on the cathode electrode in the electrocatalytic reaction system to increase solution/catalystContact area between agents, and CO is carried out on the electrolyte film 2 The electrocatalytic reduction reaction greatly improves the reaction efficiency and converts CO 2 Reducing into formic acid, ethylene, ethanol and other industrial raw materials with applicable value. The cathode electrode is Bi 2 O 3 KHCO is selected as the anolyte 3 (ii) a The anode electrode is a platinum electrode, and the cathode electrolyte is KOH; introducing CO into the cathode reactor through a gas inlet 2 Controlling the air pressure in the cathode reactor to be 2.5-3.0Mpa; and after the reaction is finished, opening a material outlet, collecting a reaction product, and detecting the concentration of the reaction product by a liquid chromatograph.
Description
Technical Field
The invention belongs to the technical field of chemical industry, and particularly relates to an electrode coating method for intermittent electrolyte for electrocatalytic reduction of CO 2 And (3) a reaction method.
Background
The industrial development and population growth consume too much fossil fuel, and due to the consumption of large amounts of fossil fuel, CO 2 The combustion end products, which are carbon materials, continue to accumulate in the atmosphere, creating a number of problems, such as the global warming effect. In response to this environmental crisis, many efforts have been made to develop clean energy sources, such as solar energy, wind energy, and biological energy, to reduce the dependence on fossil energy.
In addition to the use of clean energy, direct carbon dioxide abatement technology is also emerging, with electrochemical reduction being a very promising solution. The method uses natural sustainable energy such as wind energy, solar energy, and tidal energy to generate electric power, and drives electrochemical electrolytic cell to convert CO into CO 2 And water to value-added fuels and chemical products, known as electrical fuels. The generated electric fuel can be directly stored and utilized. CO released during reduction by electric method 2 CO released as a major waste 2 Will be captured and fed back to the reactor to allow the carbon to circulate in a closed loop. This treatment scheme can achieve CO 2 Recycle and effectively suppress CO 2 And emissions, thereby reducing the effect of greenhouse effect.
The electrochemical reduction technology successfully realizes CO 2 To effectively suppress CO 2 Emissions and reduced greenhouse effect provide new solutions. Furthermore, from electrochemical CO 2 The value-added chemical raw materials and fuels generated by reduction (CRR) can effectively reduce the dependence on the traditional fossil fuels.
Numerous researchers have conducted a large number of basic experimental studies on the efficiency of electrochemical reduction reactions and the final conversion of products. At present, a commonly used experimental medium is a solution system, the supported catalysts communicating the anode and the cathode are respectively placed in two different containers, different reaction liquids are filled in the containers, and the liquids are stirred (fig. 1), so that the contact rate of the catalysts and the solution is increased, and the generation efficiency of reaction products is improved.
As shown in fig. 1, in the electrochemical reactor which is commonly used at present, a liquid reaction solution is directly contacted with a catalyst, and then the contact area and contact efficiency between the solution and the catalyst are increased by continuously mechanically stirring the liquid phase, thereby increasing the reaction efficiency and the generation rate of the final reaction product. Temperature fields in reaction liquid in a conventional reactor can only be fixedly and uniformly distributed, and the final reactant cannot be selected in an intervention manner by changing the temperature of different areas in the same solution, so that a large amount of byproducts in the reaction cannot be effectively inhibited, and the economical efficiency of the application of the electrocatalytic reduction reaction technology is greatly weakened.
Disclosure of Invention
Based on the above problems, the present invention provides an electrode coating method for an intermittent electrolyte for an electrocatalytic reduction reaction of CO2, which can intermittently spray a liquid electrolyte membrane on a cathode electrode in an electrocatalytic reaction system, increase the contact area between the solution and a catalyst, and perform CO reduction on the electrolyte membrane 2 The electrocatalytic reduction reaction greatly improves the reaction efficiency and converts CO 2 Reducing into formic acid, ethylene, ethanol and other industrial raw materials with applicable value.
Therefore, the invention adopts the following technical scheme:
electrode coating method for intermittent electrolyte for electrocatalytic reduction of CO 2 The reaction method comprises a cathode reactor and an anode reactor, wherein the electrodes of the cathode reactor and the anode reactor are connected to a direct current power supply;
the cathode reactor is of a horizontal cylindrical sealing structure, a plurality of sheet-shaped cathode electrodes are arranged in an inner cavity of the middle and rear sections of the cathode reactor, and the cathode electrodes are vertically arranged at intervals along the length direction of the cathode reactor; the cathode electrodes are fixed on the inner wall of the cathode reactor through an insulating structure, and each cathode electrode is connected to a direct-current power supply through a lead;
a gas inlet and an electrolyte inlet are arranged at the head end of the cathode reactor, and the gas inlet is connected to a gas source through a gas conveying pipe; the electrolyte inlet is connected with an atomizing nozzle which is positioned on the axial line of the cathode reactor, and the nozzle of the atomizing nozzle faces forwards horizontally; the atomizing spray head is connected to an electrolyte pump through a guide pipe, and the electrolyte pump is connected with an electrolyte heating device; the tail end of the cathode reactor is provided with a material outlet, and the material outlet is provided with an outlet valve;
the outer wall of the cathode reactor is wrapped with a plurality of temperature control water waistcoats which are distributed at intervals along the length direction of the cathode reactor; the temperature of each temperature control water jacket is independently adjusted, and the temperature of the temperature control water jacket is gradually reduced from the head end to the tail end of the cathode reactor; the temperature of the warm water control waistcoat at the head end is not lower than 90 ℃, and the temperature of the warm water control waistcoat at the tail end is not higher than-10 ℃;
a plurality of temperature sensors are further distributed in the inner cavity of the cathode reactor along the length direction and connected to an upper computer;
the reaction method comprises the following steps:
1) The cathode electrode is Bi 2 O 3 KHCO is selected as the anolyte 3 (ii) a The anode electrode is a platinum electrode, and the cathode electrolyte is KOH;
2) Introducing CO into the cathode reactor through the gas inlet 2 Controlling the air pressure in the cathode reactor to be 2.5-3.0Mpa;
3) Starting the water jacket to adjust the temperature of the inner cavity of the cathode reactor, wherein the heat preservation time is not less than 24 hours;
4) After the heat preservation is finished, starting an electrolyte pump to inject heated KHCO into the cathode reactor 3 An electrolyte; KHCO 3 The concentration of the electrolyte is 0.48-0.52mol/L, the temperature is 95-105 ℃, the flow rate is 200-500 mL/min, the continuous injection time is controlled within 30s, then the injection is stopped, and the reaction time reaches 2min; the electrolyte pump is started again to inject KHCO 3 Controlling the continuous injection time of the electrolyte within 30s, and waiting for reaction for 2min; the reciprocating is carried out in the way;
during the reaction, the gas pressure in the cathode reactor was reduced to 2.Supplementing CO into the cathode reactor at 5Mpa 2 Gas, keeping the pressure at 2.5-3.0MPa;
under the environment of sudden temperature drop in the reactor, the high-temperature anolyte can be rapidly dispersed into water mist, and (8) the dispersed water mist is condensed into a liquid electrolyte water film on the surface of a cathode electrode in a lower temperature region (0 to 20 ℃) in the reactor;
5) And after the reaction is finished, opening a material outlet, collecting a reaction product, and detecting the concentration of the reaction product by using a liquid chromatograph.
Further, the temperature control water waistcoats comprise five, and the temperature control of the five temperature control water waistcoats from the head end to the tail end of the cathode reactor is respectively 90-degree C or more, 20-degree C, 0-degree C, -5-degree C and-10-degree C.
The 5 temperature control water jackets are filled with refrigerating fluid, and the inlet and the outlet of the refrigerating fluid are connected with external temperature control water tanks, namely, a reactor needs 5 external temperature control water tanks to be connected with the water jackets. The temperature of each temperature control water tank is independently adjusted, and the temperatures of the external temperature control water tanks are sequentially set to be 90 ℃ or more, 20 ℃, 0 ℃,5 ℃ and 10 ℃ according to the sequence from the air inlet to the air outlet; at the moment, the cold liquid temperature in the annular temperature-control water jacket structure outside the cathode reactor can basically reach the set temperature of the water tank; considering that a strong gas convection phenomenon actually exists in the reactor, the actual temperature at the position of the water waistcoat in the reactor is finally stabilized at 50 ℃, 20 ℃,10 ℃,5 ℃ and 0 ℃. Therefore, two temperature zones of high temperature at the water inlet end and low temperature at the gas outlet end and a gradient temperature dip zone with continuously dropping temperature distributed between the two temperature zones are formed in the reactor. In addition, the actual temperature in the reactor after stabilization will vary with the length of the reactor.
Further, the cathode reactor is made of stainless steel materials, the wall thickness is not less than 1cm, and the pressure-resistant degree of the inner cavity is not less than 5Mpa; the inside diameter of the cathode reactor is 20-50 cm, and the length is 300-500 cm.
Further, the cathode reactor comprises a cylinder, a head end cover plate and a tail end cover plate, wherein the head end cover plate and the tail end cover plate are fixed on the cylinder through flange structures.
Furthermore, a plurality of observation windows are arranged on the upper outer wall of the cylinder body, and the structure and the reaction condition inside the cathode reactor are checked through the observation windows.
Furthermore, the cathode electrodes are rectangular sheets, the cathode electrodes are spirally and annularly arranged along the length direction of the cathode reactor, and the adjacent cathode electrodes are mutually vertical.
Further, the length of the single cathode electrode is half of the inner diameter of the cathode reactor.
Further, the distance between the adjacent cathode electrodes is 50-500mm.
By adjusting the temperature setting of five temperature-control water waistcoats outside the reactor, a gradient temperature field which is rapidly transited from high temperature to low temperature is formed in the reactor. Then, quickly injecting the electrolyte heated at the high temperature of 100 ℃ into the reactor and filling the electrolyte with high-pressure CO 2 In a gas cathode reactor. In the cathode reactor, a gradient temperature field naturally distributed from high temperature to low temperature can instantly atomize high-temperature electrolyte to form drops of electrolyte with huge quantity and fine size, high-temperature water vapor is formed at the inlet end of the cathode reactor, and the water vapor is rapidly condensed to a liquid water film with small thickness on a sheet-shaped cathode electrode after undergoing sudden temperature drop in the reactor. At this time, the direct power supply for the reduction reaction is switched on, i.e. the surface of the water film covering the cathode electrode is subjected to the catalytic reduction reaction. After the reaction is finished, the next electrolyte injection is carried out, the reduction reaction is intermittently and periodically started, and a larger contact surface between the electrolyte and the flaky catalyst can be ensured, so that the forming efficiency of the reduction reaction and the conversion rate of a final product can be greatly improved.
The invention has the beneficial effects that: a liquid water film of the electrolyte can be intermittently formed on the surface of the sheet-shaped cathode electrode, so that the contact area of the electrolyte/the catalyst cathode electrode is greatly increased, and the catalytic reduction reaction efficiency and the final hydrate conversion efficiency are greatly improved; after the reduction reaction is finished, the next high-temperature electrolyte injection is carried out, and then the higher product conversion efficiency in the reaction process can be maintained all the time. The anolyte can be intermittently and flatly paved on the surface of a flaky cathode electrode, so that the whole catalytic reduction process can be directly carried out on a thin water film layer, and the reaction rate is higher.
Drawings
FIG. 1 is a structural view of a conventional electrochemical reaction apparatus;
FIG. 2 is a schematic diagram of the structure of a cathode reactor and an anode reactor according to the present invention;
FIG. 3 is a schematic view of the arrangement of the cathode electrode of the present invention;
in the figure: the method comprises the following steps of 1-a cathode reactor, 2-an anode reactor, 3-a direct-current power supply, 4-a temperature-controlled water vest, 5-a cathode electrode, 6-an electrolyte inlet, 7-a gas inlet, 8-a gas source, 9-a material outlet, 10-an electrolyte pump and 11-an electrolyte heating device.
Detailed Description
The invention will be further described with reference to the accompanying drawings, as shown in figures 2 and 3:
electrocatalytic reduction of CO by electrode coating method of intermittent electrolyte 2 The reaction method comprises a cathode reactor 1 and an anode reactor 2, wherein the electrodes of the cathode reactor 1 and the anode reactor 2 are connected to a direct current power supply 3;
the cathode reactor 1 is of a horizontal cylindrical sealing structure, a plurality of sheet-shaped cathode electrodes 5 are arranged in an inner cavity of the middle rear section of the cathode reactor 1, and the cathode electrodes 5 are vertically arranged at intervals along the length direction of the cathode reactor 1; the cathode electrodes 5 are fixed on the inner wall of the cathode reactor 1 through an insulating structure, and each cathode electrode 5 is connected to the direct current power supply 3 through a lead;
a gas inlet 7 and an electrolyte inlet 6 are arranged at the head end of the cathode reactor 1, and the gas inlet 7 is connected to a gas source 8 through a gas conveying pipe; the electrolyte inlet 6 is connected with an atomizing nozzle which is positioned on the axial line of the cathode reactor 1, and the nozzle of the atomizing nozzle faces forwards horizontally; the atomizing spray head is connected to an electrolyte pump 10 through a guide pipe, and the electrolyte pump 10 is connected with an electrolyte heating device 11; the tail end of the cathode reactor 1 is provided with a material outlet 9, and the material outlet 9 is provided with an outlet valve;
the outer wall of the cathode reactor 1 is wrapped with a plurality of temperature control water waistcoats 4, and the temperature control water waistcoats 4 are distributed at intervals along the length direction of the cathode reactor 1; each temperature control water jacket 4 is independently adjusted, and the temperature of the temperature control water jacket 4 is gradually reduced from the head end to the tail end of the cathode reactor 1; the temperature of the temperature-controlled water waistcoat 4 at the head end is not lower than 90 ℃, and the temperature of the temperature-controlled water waistcoat 4 at the tail end is not higher than-10 ℃;
and a plurality of temperature sensors are further distributed in the inner cavity of the cathode reactor 1 along the length direction and connected to an upper computer.
The reaction method comprises the following steps:
1) The cathode 5 is Bi 2 O 3 KHCO is selected as the anolyte 3 (ii) a The anode electrode is a platinum electrode, and the cathode electrolyte is KOH.
2) CO is introduced into the cathode reactor 1 via the gas inlet 7 2 Controlling the air pressure in the cathode reactor 1 to be 2.5-3.0Mpa.
3) And (3) starting the water jacket to adjust the temperature of the inner cavity of the cathode reactor 1, wherein the heat preservation time is not less than 24 hours.
4) After the heat preservation is finished, the electrolyte pump 10 is started to inject the heated KHCO into the cathode reactor 1 3 An electrolyte; KHCO 3 The concentration of the electrolyte is 0.48-0.52mol/L, the temperature is 95-105 ℃, the flow rate is 200-500 mL/min, the continuous injection time is controlled within 30s, then the injection is stopped, and the reaction time is up to 2min; the electrolyte pump 10 is restarted to inject the KHCO 3 Controlling the continuous injection time of the electrolyte within 30s, and waiting for reaction for 2min; the reciprocating is carried out in the way;
in the reaction process, when the air pressure in the cathode reactor 1 is reduced to 2.5 Mpa, CO is supplemented into the cathode reactor 1 2 Gas, the pressure is maintained at 2.5-3.0MPa.
5) After the reaction is finished, the material outlet 9 is opened, the reaction product is collected, and the concentration of the reaction product is detected by a liquid chromatograph.
Claims (8)
1. Electrocatalytic reduction of CO by electrode coating method of intermittent electrolyte 2 The reaction method is characterized by comprising a cathode reactor and an anode reactor, wherein the electrodes of the cathode reactor and the anode reactor are connected to a direct current power supply;
the cathode reactor is of a horizontal cylindrical sealing structure, a plurality of sheet-shaped cathode electrodes are arranged in an inner cavity of the middle and rear sections of the cathode reactor, and the cathode electrodes are vertically arranged at intervals along the length direction of the cathode reactor; the cathode electrodes are fixed on the inner wall of the cathode reactor through an insulating structure, and each cathode electrode is connected to a direct-current power supply through a lead;
a gas inlet and an electrolyte inlet are arranged at the head end of the cathode reactor, and the gas inlet is connected to a gas source through a gas conveying pipe; the electrolyte inlet is connected with an atomizing nozzle which is positioned on the axial line of the cathode reactor, and the nozzle of the atomizing nozzle faces forwards horizontally; the atomizing nozzle is connected to an electrolyte pump through a guide pipe, and the electrolyte pump is connected with an electrolyte heating device; the tail end of the cathode reactor is provided with a material outlet, and the material outlet is provided with an outlet valve;
the outer wall of the cathode reactor is wrapped with a plurality of temperature control water waistcoats which are distributed at intervals along the length direction of the cathode reactor; the temperature of each temperature control water jacket is adjusted independently, and the temperature of the temperature control water jacket is gradually reduced from the head end to the tail end of the cathode reactor; the temperature of the warm water control waistcoat at the head end is not lower than 90 ℃, and the temperature of the warm water control waistcoat at the tail end is not higher than-10 ℃;
a plurality of temperature sensors are further distributed in the inner cavity of the cathode reactor along the length direction and are connected to an upper computer;
the reaction method comprises the following steps:
1) The cathode electrode is Bi 2 O 3 KHCO is selected as the anolyte 3 (ii) a The anode electrode is a platinum electrode, and the cathode electrolyte is KOH;
2) Introducing CO into the cathode reactor through the gas inlet 2 Controlling the air pressure in the cathode reactor to be 2.5-3.0Mpa;
3) Starting the water jacket to adjust the temperature of the inner cavity of the cathode reactor, wherein the heat preservation time is not less than 24 hours;
4) After the heat preservation is finished, starting an electrolyte pump to inject heated KHCO into the cathode reactor 3 An electrolyte; KHCO 3 The concentration of the electrolyte is 0.48-0.52mol/L, the temperature is 95-105 ℃, the flow rate is 200-500 mL/min, the continuous injection time is controlled within 30s, then the injection is stopped, and the reaction time reaches 2min; restart againMoving electrolyte pump for KHCO injection 3 Controlling the continuous injection time of the electrolyte within 30s, and waiting for reaction for 2min; so as to reciprocate;
in the reaction process, when the air pressure in the cathode reactor is reduced to 2.5 Mpa, CO is supplemented into the cathode reactor 2 Gas, keeping the pressure at 2.5-3.0MPa;
5) And after the reaction is finished, opening a material outlet, collecting a reaction product, and detecting the concentration of the reaction product by a liquid chromatograph.
2. The method for electrocatalytic reduction of CO by electrode coating of a batch-type electrolyte according to claim 1 2 The reaction method is characterized in that the temperature control water waistcoats include five, and the temperature control of the five temperature control water waistcoats from the head end to the tail end of the cathode reactor is respectively 90 ℃ or more, 20 ℃, 0 ℃,5 ℃ and 10 ℃.
3. The method for electrocatalytic reduction of CO by electrode coating of a batch-type electrolyte according to claim 1 2 The reaction method is characterized in that the cathode reactor is made of stainless steel materials, the wall thickness is not less than 1cm, and the pressure-resistant degree of an inner cavity is not less than 5Mpa; the inside diameter of the cathode reactor is 20-50 cm, and the length is 300-500 cm.
4. The method for electrocatalytic reduction of CO by electrode coating of a batch-type electrolyte according to claim 3 2 The reaction method is characterized in that the cathode reactor comprises a cylinder, a head end cover plate and a tail end cover plate, wherein the head end cover plate and the tail end cover plate are fixed on the cylinder through flange structures.
5. The method for electrocatalytic reduction of CO by electrode coating of a batch electrolyte according to claim 4 2 The reaction method is characterized in that a plurality of observation windows are arranged on the upper outer wall of the cylinder body, and the structure and the reaction condition in the cathode reactor are checked through the observation windows.
6. The method for electrocatalytic reduction of a batch electrolyte according to claim 1 by electrode coatingCO 2 The reaction method is characterized in that the cathode electrodes are rectangular sheets, the cathode electrodes are spirally and annularly arranged along the length direction of the cathode reactor, and the adjacent cathode electrodes are mutually vertical.
7. The method for electrocatalytic reduction of CO by electrode coating of a batch-type electrolyte according to claim 6 2 Reaction process characterized in that the length of the single cathode electrode is half of the internal diameter of the cathode reactor.
8. The method for electrocatalytic reduction of CO by electrode coating of a batch-type electrolyte according to claim 7 2 The reaction method is characterized in that the distance between adjacent cathode electrodes is 50-500mm.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210586106.9A CN115198289B (en) | 2022-05-27 | 2022-05-27 | Electrocatalytic reduction of CO by electrode coating method of intermittent electrolyte 2 Reaction method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210586106.9A CN115198289B (en) | 2022-05-27 | 2022-05-27 | Electrocatalytic reduction of CO by electrode coating method of intermittent electrolyte 2 Reaction method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN115198289A true CN115198289A (en) | 2022-10-18 |
| CN115198289B CN115198289B (en) | 2023-03-14 |
Family
ID=83576092
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202210586106.9A Active CN115198289B (en) | 2022-05-27 | 2022-05-27 | Electrocatalytic reduction of CO by electrode coating method of intermittent electrolyte 2 Reaction method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN115198289B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115672020A (en) * | 2022-12-12 | 2023-02-03 | 中国科学院西北生态环境资源研究院 | Device for capturing, separating and catalyzing carbon dioxide in flue waste gas and control method thereof |
Citations (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2006111924A (en) * | 2004-10-14 | 2006-04-27 | Honda Motor Co Ltd | High pressure hydrogen production device |
| CN103154323A (en) * | 2010-10-15 | 2013-06-12 | 能源及环境研究中心基金会 | Electrochemical process for the preparation of nitrogen fertilizers |
| JP5347080B1 (en) * | 2013-05-07 | 2013-11-20 | 株式会社センリョウ | Temperature difference power ship |
| US20160053388A1 (en) * | 2013-04-08 | 2016-02-25 | Commissariat A L'energie Atomique Et Aux Energies Alternatives | Methods for producing combustible gas from the electrolysis of water (hte) or co-electrolysis with h2o/co2 in the same chamber, and associated catalytic reactor and system |
| CN110117794A (en) * | 2019-05-21 | 2019-08-13 | 盐城工学院 | A kind of electroreduction CO2The three Room type electrolytic cell devices and its electrolytic method of formates processed |
| US20200002823A1 (en) * | 2018-03-20 | 2020-01-02 | Kabushiki Kaisha Toshiba | Carbon dioxide electrolytic system |
| CN112593251A (en) * | 2019-09-17 | 2021-04-02 | 株式会社东芝 | Electrochemical reaction device |
| CN112853389A (en) * | 2021-01-15 | 2021-05-28 | 中国科学院上海应用物理研究所 | Electrochemical synthesis device based on high-temperature high-pressure electrolysis technology |
| CN113373462A (en) * | 2021-05-21 | 2021-09-10 | 南京理工大学 | For electrochemical reduction of CO2Membrane type liquid flow electrolytic cell and testing process |
| CN113862720A (en) * | 2021-08-25 | 2021-12-31 | 天津大学 | Metal Cu thin film electrode capable of selectively exposing (100) crystal face and preparation method thereof |
| WO2022020950A1 (en) * | 2020-07-28 | 2022-02-03 | Électro Carbone Inc. | Electrochemical cell for carbon dioxide reduction towards liquid chemicals |
-
2022
- 2022-05-27 CN CN202210586106.9A patent/CN115198289B/en active Active
Patent Citations (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2006111924A (en) * | 2004-10-14 | 2006-04-27 | Honda Motor Co Ltd | High pressure hydrogen production device |
| CN103154323A (en) * | 2010-10-15 | 2013-06-12 | 能源及环境研究中心基金会 | Electrochemical process for the preparation of nitrogen fertilizers |
| US20160053388A1 (en) * | 2013-04-08 | 2016-02-25 | Commissariat A L'energie Atomique Et Aux Energies Alternatives | Methods for producing combustible gas from the electrolysis of water (hte) or co-electrolysis with h2o/co2 in the same chamber, and associated catalytic reactor and system |
| JP5347080B1 (en) * | 2013-05-07 | 2013-11-20 | 株式会社センリョウ | Temperature difference power ship |
| US20200002823A1 (en) * | 2018-03-20 | 2020-01-02 | Kabushiki Kaisha Toshiba | Carbon dioxide electrolytic system |
| CN110117794A (en) * | 2019-05-21 | 2019-08-13 | 盐城工学院 | A kind of electroreduction CO2The three Room type electrolytic cell devices and its electrolytic method of formates processed |
| CN112593251A (en) * | 2019-09-17 | 2021-04-02 | 株式会社东芝 | Electrochemical reaction device |
| WO2022020950A1 (en) * | 2020-07-28 | 2022-02-03 | Électro Carbone Inc. | Electrochemical cell for carbon dioxide reduction towards liquid chemicals |
| CN112853389A (en) * | 2021-01-15 | 2021-05-28 | 中国科学院上海应用物理研究所 | Electrochemical synthesis device based on high-temperature high-pressure electrolysis technology |
| CN113373462A (en) * | 2021-05-21 | 2021-09-10 | 南京理工大学 | For electrochemical reduction of CO2Membrane type liquid flow electrolytic cell and testing process |
| CN113862720A (en) * | 2021-08-25 | 2021-12-31 | 天津大学 | Metal Cu thin film electrode capable of selectively exposing (100) crystal face and preparation method thereof |
Non-Patent Citations (2)
| Title |
|---|
| 张琪;许武韬;刘予宇;张久俊;: "二氧化碳电化学还原概述" * |
| 陈庆国等: "一种二酰胺基吡啶季铵盐的合成及其缓蚀性能" * |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115672020A (en) * | 2022-12-12 | 2023-02-03 | 中国科学院西北生态环境资源研究院 | Device for capturing, separating and catalyzing carbon dioxide in flue waste gas and control method thereof |
| CN115672020B (en) * | 2022-12-12 | 2023-02-28 | 中国科学院西北生态环境资源研究院 | Device for capturing, separating and catalyzing carbon dioxide in flue waste gas and control method thereof |
Also Published As
| Publication number | Publication date |
|---|---|
| CN115198289B (en) | 2023-03-14 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105084311B (en) | The methanol-water hydrogen production system employing reforming technology and its application and hydrogen production process of a kind of zero carbon emission | |
| US7615138B2 (en) | Electrolysis apparatus with pulsed, dual voltage, multi-composition electrode assembly | |
| CN107313068A (en) | A kind of electrochemical method of synthetic acidic hydrogen peroxide | |
| CN115198289B (en) | Electrocatalytic reduction of CO by electrode coating method of intermittent electrolyte 2 Reaction method | |
| CN102400169A (en) | Method for producing hydrogen by alkalescent microbe electrolysis | |
| WO2014160301A1 (en) | Method and apparatus for generating hydrogen from metal | |
| US11905503B2 (en) | Electromethanogenesis reactor | |
| CN110820007A (en) | PBI proton exchange membrane electrolysis module and seawater electrolysis hydrogen production device | |
| CN105200448A (en) | Electrochemistry hydrogen pump dual reactor for organic matter dehydrogenation and hydrogenation coupling | |
| Bajracharya et al. | Advances in cathode designs and reactor configurations of microbial electrosynthesis systems to facilitate gas electro-fermentation | |
| Nelabhotla et al. | Power-to-gas for methanation | |
| CN116732572A (en) | Electrocatalytic coupling biocatalysis reaction integrated device and CO 2 Method of utilization | |
| CN114540852B (en) | Carbon dioxide electroreduction bionic electrolytic cell and operation method thereof | |
| CN101314572A (en) | Method for preparing tetramethyl ammonium hydrogen carbonate with condensation reaction of pipe type reactor | |
| CN112299371A (en) | Hydrogen supply system and hydrogen supply method | |
| Wang et al. | Kinetics and mechanism of reduction of CO2 by glycerol under alkaline hydrothermal conditions | |
| CN111850592B (en) | Method for co-producing propionic acid and improving electrolytic water performance of anion exchange membrane | |
| CN212103028U (en) | PBI proton exchange membrane electrolysis module and seawater electrolysis hydrogen production device | |
| CN216457951U (en) | Electrolytic device and CO2Digestion system | |
| CN215713422U (en) | Automatic carbon dioxide reduction equipment for waste gas utilization | |
| WO2014101864A1 (en) | Low-temperature liquid fuel reforming hydrogen generator and preparation method for high-purity hydrogen | |
| CN113828126A (en) | Electrolysis device and CO2Digestion system | |
| CN113969410B (en) | Method for synthesizing 2, 5-dihydroxymethyl furan by electrocatalytic hydrogenation of 5-hydroxymethylfurfural by adopting non-noble metal oxide | |
| US11421330B2 (en) | Methods for carbon dioxide hydrogenation | |
| CN104831308A (en) | High-efficiency thermoelectrical chemical hydrogen production device, and hydrogen production method |
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 | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |