阅读说明：本技术 一种煤矿风排瓦斯低浓度甲烷氧化脱除系统 (Coal mine air-discharging gas low-concentration methane oxidation removal system ) 是由 祁志福 丁浩然 骆周扬 厉宸希 申震 罗海华 孙士恩 韩龙 于 2021-03-12 设计创作，主要内容包括：本发明涉及一种煤矿风排瓦斯低浓度甲烷氧化脱除系统,包括：引风除尘装置、甲烷氧化反应器、碳捕集反应器、钙基吸附剂供料器和热交换器；引风除尘装置与甲烷氧化反应器通过风道连接,将矿井瓦斯气进行初步的除尘过滤后不断输送至甲烷氧化反应器的内部,甲烷氧化反应器通过气道连接碳捕集反应器,碳捕集反应器还连接钙基吸附剂供料器(可以实现连续进料和反应后吸收剂回收,保持床层内具备足量的钙基吸收剂进行碳捕集反应),甲烷氧化反应器还通过气道连接热交换器。本发明的有益效果是：本发明与现有设备相比,能够显著提高能量利用率、减少能耗和充分进行物质利用,同时具备结构紧凑、适用性强等特点。(The invention relates to a coal mine wind exhaust gas low-concentration methane oxidation removal system, which comprises: the system comprises an induced draft dust removal device, a methane oxidation reactor, a carbon capture reactor, a calcium-based adsorbent feeder and a heat exchanger; the induced air dust removal device is connected with the methane oxidation reactor through an air duct, mine gas is subjected to preliminary dust removal and filtration and then is continuously conveyed to the interior of the methane oxidation reactor, the methane oxidation reactor is connected with the carbon capture reactor through an air duct, the carbon capture reactor is further connected with a calcium-based adsorbent feeder (continuous feeding and recovery of an absorbent after reaction can be realized, and sufficient calcium-based absorbent is kept in a bed layer for carrying out carbon capture reaction), and the methane oxidation reactor is further connected with a heat exchanger through an air duct. The invention has the beneficial effects that: compared with the existing equipment, the invention can obviously improve the energy utilization rate, reduce the energy consumption and fully utilize the substances, and has the characteristics of compact structure, strong applicability and the like.)

1. The utility model provides a coal mine wind gas discharge low concentration methane oxidation desorption system which characterized in that includes: the system comprises an induced draft dust removal device (1), a methane oxidation reactor (2), a carbon capture reactor (3), a calcium-based adsorbent feeder (4) and a heat exchanger (5); the induced air dust removal device (1) is connected with the methane oxidation reactor (2) through an air duct, the methane oxidation reactor (2) is connected with the carbon capture reactor (3) through an air duct, the carbon capture reactor (3) is also connected with a calcium-based adsorbent feeder (4), and the methane oxidation reactor (2) is also connected with a heat exchanger (5) through an air duct;

the methane oxidation reactor (2) is filled with a catalyst, and the carbon capture reactor (3) is filled with a calcium-based absorbent.

2. The system for oxidizing and removing low-concentration methane in coal mine air discharge gas as claimed in claim 1, wherein: an induction heating device is arranged on the bed layer of the catalyst; the reaction temperature range of the catalyst is 300-450 ℃.

3. The system for oxidizing and removing low-concentration methane in coal mine air discharge gas as claimed in claim 1, wherein: the catalyst is a honeycomb ceramic supported catalyst.

4. The system for oxidizing and removing low-concentration methane in coal mine air discharge gas as claimed in claim 3, wherein: the honeycomb ceramic supported catalyst comprises the components of nano copper oxide, stainless steel particles and cordierite honeycomb ceramic; wherein the weight percentage of the nano copper oxide is 10-20%, the weight percentage of the stainless steel particles is 10-30%, and the weight percentage of the cordierite honeycomb ceramic is 50-80%; the nano copper oxide is used as an oxidation reaction catalyst, the stainless steel particles are used as a heating body, and the cordierite honeycomb ceramic is used as a carrier material.

5. The system for oxidizing and removing low-concentration methane in coal mine air discharge gas as claimed in claim 3, wherein: the components of the honeycomb ceramic supported catalyst are 15% of nano copper oxide, 30% of stainless steel particles and 55% of cordierite honeycomb ceramic.

6. The system for oxidizing and removing low-concentration methane in coal mine air discharge gas as claimed in claim 1, wherein: the reaction temperature range of the calcium-based absorbent is 80-200 ℃.

7. The construction method of the coal mine wind methane-discharging low-concentration methane oxidation removal system according to claim 1, characterized by comprising the following steps:

step 1, preparing a catalyst;

step 1.1, first, preparing Cu (NO)₃)₂Solution, ammonia water and NaOH solution; then Cu (NO) is added under the conditions of set temperature and stirring₃)₂Slowly dropwise adding ammonia water into the solution; then, dropwise adding the prepared NaOH solution into the obtained mixed solution until the pH value of the mixed solution is 9-10 to obtain a blue suspended precursor solution; finally, carrying out centrifugal precipitation for multiple times, removing supernatant liquor after each centrifugation, and supplementing deionized water according to the same volume of the removed supernatant liquor;

step 1.2, taking the blue suspension precursor solution prepared in the step 1.1, and obtaining blue precipitate slurry through centrifugal precipitation; transferring the blue precipitate slurry into a reaction kettle, heating to a set temperature at a certain heating rate, and preserving heat; after cooling the blue precipitate slurry in the reaction kettle, carrying out centrifugal separation on the generated black slurry and drying to obtain black powder, wherein the black powder is a nano copper oxide catalyst;

step 1.3, placing stainless steel particles into a polyethylene glycol solution, soaking cordierite honeycomb ceramics in the polyethylene glycol solution added with the stainless steel particles for a period of time under the condition of stirring, taking out the cordierite honeycomb ceramics, drying the cordierite honeycomb ceramics, and then performing high-temperature calcination treatment in times;

step 1.4, mixing the black powder prepared in the step 1.2 with absolute ethyl alcohol, putting the cordierite honeycomb ceramic prepared in the step 1.3 into a mixed solution of the black powder and the absolute ethyl alcohol under the condition of stirring for dipping treatment, and then drying again to obtain a catalyst;

step 2, preparing a calcium-based absorbent, wherein the calcium-based absorbent is calcium oxide;

step 2.1, taking Ca (OH)₂Mixing the powder with a polyethylene glycol aqueous solution at normal temperature to form a viscous block, then putting the viscous block into an extruder, and extruding the viscous block to form a strip-shaped precursor product;

2.2, putting the strip-shaped precursor extruded and formed in the step 2.1 into a rounding machine, and rotating the rounding machine to form a granular product by the strip-shaped precursor under the action of force;

and 2.3, drying the particle product formed in the step 2.2, and then calcining to obtain the calcium-based absorbent.

8. The construction method of the coal mine wind methane discharge low-concentration methane oxidation removal system according to claim 7, characterized in that:

step 1.1 Cu (NO)₃)₂The molar concentrations of the solution, the ammonia water and the NaOH solution are respectively 0.5mmol/L, 0.15mol/L and 1 mol/L; the set temperature was 50 ℃ and ammonia and Cu (NO)₃)₂The volume ratio of the solution is controlled to be 3: 10; the number of times of centrifugal separation was 5;

in the step 1.2, the centrifugal rotating speed is 8000rpm when the blue suspension precursor solution is centrifuged, and the centrifugal time is 5min each time; the heating rate of the blue precipitation slurry in the reaction kettle is 5 ℃/min, the set temperature is 130 ℃, and the heat preservation time is 10 hours; the centrifugal rotation speed of the black slurry generated after the blue precipitate slurry in the reaction kettle is cooled is 10000rpm when the black slurry is subjected to centrifugal separation, and the centrifugal time is 10min each time; the drying time of the black slurry is 24 hours, and the drying temperature is 80 ℃;

in the step 1.3, the stainless steel particles are 200-300 meshes; the concentration of the polyethylene glycol solution is 1 mol/L; the immersion time of the cordierite honeycomb ceramic in the polyethylene glycol solution added with the stainless steel particles is 2 hours; the drying temperature of the impregnated cordierite honeycomb ceramic is 105-130 ℃, and the drying time is 12 h; the temperature of the high-temperature calcination treatment is 400 ℃, and the calcination time is 3 h;

in the step 1.4, the concentration of the black powder in the mixed solution of the black powder and the absolute ethyl alcohol is 0.1-0.3 mol/L.

9. The construction method of the coal mine wind methane discharge low-concentration methane oxidation removal system according to claim 7, characterized in that:

in the step 2.1, the concentration of polyethylene glycol in the polyethylene glycol aqueous solution is 1-2 mol/L, and the diameter of the strip-shaped precursor product is 2-3 mm;

in the step 2.2, the rotating speed of the rounding machine is 60rpm, and the rotating time is 60 min; the diameter of the particle product is 2-3 mm;

the drying time in the step 2.3 is 24 hours, and the drying temperature is 80-105 ℃; the temperature of the calcination treatment was 700 ℃ and the duration of the calcination treatment was 3 hours.

Technical Field

The invention belongs to the technical field related to energy utilization equipment, and particularly relates to a coal mine air exhaust gas low-concentration methane oxidation removal system based on catalytic oxidation and carbon capture processes.

Background

The underground mining is a main means for coal production in China, and coal mine gas (coal bed gas) released in the mining process is easy to cause gas accidents, so that great potential safety hazards are caused in the coal mine production process. Various policy regulations have been provided by the nation to prescribe coal mine gas drainage, enhance coal mine gas control and promote coal mine gas cleaning.

In relevant regulations, the gas emission of underground coal mines is divided into gas drainage and air discharge, the concentration of methane in the gas drainage is generally higher than 30%, the concentration of methane in the gas drainage before mining can reach more than 90%, and the low-concentration gas drainage can be purified by technical means such as pressure swing adsorption and the like and then utilized, and is mainly used for civil gas, gas power generation and other industrial purposes. However, the concentration of the air-exhaust gas discharged by ventilation is generally lower than 0.5%, the effective utilization of the air-exhaust gas is difficult, and the discharge cannot be reduced in order to ensure the safety of a coal mine.

The regulations of coal mine safety regulations stipulate that the methane concentration of a gas coal mine ventilation wellhead must be lower than 0.75% in order to ensure the safety of coal mine production. According to the relevant regulations, the amount of wind-blown gas in national emphasis coal mines has exceeded 60 billionths of a cubic meter by 2007, and due to its lower methane concentration, it is now mainly emitted directly into the atmosphere causing relatively large greenhouse gas pollution.

Therefore, in the coal mining process of China, a large amount of gas is directly discharged into the atmosphere without being treated. While the greenhouse effect of methane is about CO₂28 times of the current society, under the condition that the current society is increasingly concerned about environmental protection, the emission control of coal mine gas becomes more and more important. At the same time, efforts are being made worldwide to drive the carbon neutralization, non-CO of gas emission processes₂The carbon capture process is also a very important area.

More specifically, the analysis is carried out, in the prior art, the greenhouse gas emission control is not effectively carried out on the coal mine wind exhaust gas with the methane concentration lower than 0.75%, and along with the gradual increase of the requirement of the whole society for environmental protection, how to cleanly and efficiently realize the coal mine wind exhaust gas emission control requirement and design the aspects such as a matched composition system and a working mode thereof are becoming the technical problems to be solved urgently in the field.

Disclosure of Invention

The invention aims to overcome the defects in the prior art and provides a coal mine air exhaust gas low-concentration methane oxidation removal system.

This kind of coal mine wind is arranged gas low concentration methane and is oxidized desorption system includes: the system comprises an induced draft dust removal device, a methane oxidation reactor, a carbon capture reactor, a calcium-based adsorbent feeder and a heat exchanger; the induced air dust removal device is connected with the methane oxidation reactor through an air duct, mine gas is subjected to preliminary dust removal and filtration and then is continuously conveyed into the methane oxidation reactor, the methane oxidation reactor is connected with the carbon capture reactor through an air duct, the carbon capture reactor is also connected with a calcium-based adsorbent feeder (the continuous feeding and the recovery of an absorbent after reaction can be realized, and a sufficient amount of calcium-based absorbent is kept in a bed layer for carrying out the carbon capture reaction), and the methane oxidation reactor is also connected with a heat exchanger through an air duct; the methane oxidation reactor is filled with a catalyst, and the carbon capture reactor is filled with a calcium-based absorbent.

Preferably, an induction heating device is arranged on the bed layer of the catalystHeating and supplying energy by adopting an induction heating mode; the reaction temperature range of the catalyst is 300-450 ℃, when the catalyst is preheated to a first specified temperature (400 ℃) by high-frequency induction heating, gas input from the outside contacts the catalyst and generates methane oxidation reaction, and methane in the gas reacts to generate H₂O and CO₂And the product gas after the reaction continues to enter a carbon capture reactor to carry out a carbon capture reaction process.

Preferably, the catalyst is a honeycomb ceramic supported catalyst, the size of the pore channel of the honeycomb ceramic supported catalyst is adjustable, and the flow resistance is controllable.

Preferably, the components of the honeycomb ceramic supported catalyst are nano copper oxide, 316 stainless steel particles and cordierite honeycomb ceramic; wherein the mass percent of the nano copper oxide is 10-20%, the mass percent of the 316 stainless steel particles is 10-30%, and the mass percent of the cordierite honeycomb ceramic is 50-80%; the nano copper oxide is used as an oxidation reaction catalyst, 316 stainless steel particles are used as a heating body, and cordierite honeycomb ceramic is used as a carrier material.

Preferably, the components of the honeycomb ceramic supported catalyst are 15% of nano copper oxide, 30% of 316 stainless steel particles and 55% of cordierite honeycomb ceramic, and the percentages refer to mass percent.

Preferably, the reaction temperature of the calcium-based absorbent is 80-200 ℃, and after the carbon capture reactor reaches a second specified temperature (120 ℃), the carbon capture reactor is oxidized by CO-containing gas output from the methane oxidation reactor₂The gas contact reaction can effectively absorb CO₂(ii) a The product gas after the reaction in the methane oxidation reactor passes through the heat exchanger, and the product gas is cooled, and the heat exchanger transfers heat to the inlet of the methane oxidation reactor to preheat the inlet gas, so that the energy-saving effect is achieved.

The construction method of the coal mine air-exhaust gas low-concentration methane oxidation removal system specifically comprises the following steps:

step 1, preparing a catalyst;

step 1.1, first, preparing Cu (NO)₃)₂Solution, ammonia water and NaOH solution; then the mixture is stirred at a set temperatureCu(NO₃)₂Slowly dropwise adding ammonia water into the solution; then, dropwise adding the prepared NaOH solution into the obtained mixed solution until the pH value of the mixed solution is 9-10 to obtain a blue suspended precursor solution; finally, carrying out centrifugal precipitation for multiple times, removing supernatant liquor after each centrifugation, and supplementing deionized water according to the same volume of the removed supernatant liquor;

step 1.2, taking the blue suspension precursor solution prepared in the step 1.1, and obtaining blue precipitate slurry through centrifugal precipitation; transferring the blue precipitate slurry into a reaction kettle, heating to a set temperature at a certain heating rate, and preserving heat; after cooling the blue precipitate slurry in the reaction kettle, carrying out centrifugal separation on the generated black slurry and drying to obtain black powder, wherein the black powder is a nano copper oxide catalyst;

step 1.3, putting 316 stainless steel particles into a polyethylene glycol solution, soaking cordierite honeycomb ceramic in the polyethylene glycol solution added with the stainless steel particles for a period of time under the condition of stirring, taking out the cordierite honeycomb ceramic, drying the cordierite honeycomb ceramic, and then carrying out high-temperature calcination treatment in times;

step 1.4, mixing the black powder prepared in the step 1.2 with absolute ethyl alcohol, putting the cordierite honeycomb ceramic prepared in the step 1.3 into a mixed solution of the black powder and the absolute ethyl alcohol under the condition of stirring for impregnation treatment, and then drying again to obtain a catalyst (a required oxygen carrier product);

step 2, preparing a calcium-based absorbent, wherein the calcium-based absorbent is calcium oxide;

step 2.1, taking Ca (OH)₂Mixing the powder with a polyethylene glycol aqueous solution at normal temperature to form a viscous block, then putting the viscous block into an extruder, and extruding the viscous block to form a strip-shaped precursor product;

2.2, putting the strip-shaped precursor extruded and formed in the step 2.1 into a rounding machine, and rotating the rounding machine to form a granular product by the strip-shaped precursor under the action of force;

and 2.3, drying the particle product formed in the step 2.2, and then calcining to obtain the calcium-based absorbent.

Preferably, Cu (NO) in step 1.1₃)₂The molar concentrations of the solution, the ammonia water and the NaOH solution are respectively 0.5mmol/L, 0.15mol/L and 1 mol/L; the set temperature was 50 ℃ and ammonia and Cu (NO)₃)₂The volume ratio of the solution is controlled to be 3: 10; the number of times of centrifugal separation was 5; in the step 1.2, the centrifugal rotating speed is 8000rpm when the blue suspension precursor solution is centrifuged, and the centrifugal time is 5min each time; the heating rate of the blue precipitation slurry in the reaction kettle is 5 ℃/min, the set temperature is 130 ℃, and the heat preservation time is 10 hours; the centrifugal rotation speed of the black slurry generated after the blue precipitate slurry in the reaction kettle is cooled is 10000rpm when the black slurry is subjected to centrifugal separation, and the centrifugal time is 10min each time; the drying time of the black slurry is 24 hours, and the drying temperature is 80 ℃; in the step 1.3, the stainless steel particles are 200-300 meshes; the concentration of the polyethylene glycol solution is 1 mol/L; the immersion time of the cordierite honeycomb ceramic in the polyethylene glycol solution added with the stainless steel particles is 2 hours; the drying temperature of the impregnated cordierite honeycomb ceramic is 105-130 ℃, and the drying time is 12 h; the temperature of the high-temperature calcination treatment is 400 ℃, and the calcination time is 3 h; in the step 1.4, the concentration of the black powder in the mixed solution of the black powder and the absolute ethyl alcohol is 0.1-0.3 mol/L.

Preferably, in the step 2.1, the concentration of polyethylene glycol in the polyethylene glycol aqueous solution is 1-2 mol/L, and the diameter of the strip-shaped precursor product is 2-3 mm; in the step 2.2, the rotating speed of the rounding machine is 60rpm, and the rotating time is 60 min; the diameter of the particle product is 2-3 mm; the drying time in the step 2.3 is 24 hours, and the drying temperature is 80-105 ℃; the temperature of the calcination treatment was 700 ℃ and the duration of the calcination treatment was 3 hours.

The invention has the beneficial effects that:

compared with the existing equipment, the system can remarkably improve the energy utilization rate, reduce the energy consumption and fully utilize substances, and has the characteristics of compact structure, strong applicability and the like;

according to the invention, by researching and designing the type of the key catalyst, the key process conditions of the reaction route and the like, compared with the existing preparation process mode, the method not only can realize the methane oxidation reaction with high selectivity and high reactivity, but also effectively improves the response speed and the energy utilization rate;

the technological process of the catalyst preparation of the invention is convenient to control, the reaction rate is high, the product performance is excellent, and the methane oxidation reaction conversion rate higher than 99% can be obtained under the reaction condition lower than 400 ℃.

Drawings

FIG. 1 is a schematic view of the overall construction of a coal mine gas low-concentration methane oxidation removal system;

FIG. 2 is a schematic process flow diagram for preparing a honeycomb ceramic catalyst;

fig. 3 is a schematic process flow diagram for the preparation of a calcium based absorbent.

Description of reference numerals: the system comprises an induced draft dust removal device 1, a methane oxidation reactor 2, a carbon capture reactor 3, a calcium-based adsorbent feeder 4 and a heat exchanger 5.

Detailed Description

The present invention will be further described with reference to the following examples. The following examples are set forth merely to aid in the understanding of the invention. It should be noted that, for a person skilled in the art, several modifications can be made to the invention without departing from the principle of the invention, and these modifications and modifications also fall within the protection scope of the claims of the present invention.

According to the invention, methane is oxidized into carbon dioxide and water at low temperature through the methane oxidation reactor, carbon dioxide is captured and collected through the carbon capture reactor, heat required in the methane oxidation reaction process supplies energy to an oxidation reaction catalyst through an induction heating mode, gas after reaction is introduced into the carbon capture reactor to capture generated carbon dioxide, and the calcium adsorbent feeder continuously updates the calcium adsorbent in the carbon capture reactor. The invention also designs the catalyst and the carbon dioxide adsorbent applied by the system in a targeted manner. The invention can realize the processes of low-cost, high-energy utilization rate and environment-friendly oxidation removal and carbon capture of low-concentration methane in the gas under the conditions of low energy consumption, quick start and high dynamic response, and has compact equipment and flexible and convenient operation.

Example 1:

the overall structure schematic diagram of the low-concentration methane oxidation removal system for the coal mine wind-exhaust gas is shown in figure 1, and the low-concentration methane oxidation removal process mainly realizes the CO generation of methane through the methane oxidation reaction on the surface of a catalyst₂And H₂O, by simultaneous CO-entrainment₂The reacted gas reacts with the calcium absorbent to remove CO in the gas₂The reaction is trapped in the calcium carbonate product. The reaction process comprises the following steps:

a methane oxidation reactor: CH (CH)₄+2O₂→CO₂+2H₂O

A carbon capture reactor: CO 2₂+CaO→CaCO₃

On the methane oxidation catalyst designed in this example, the reaction activity and the reaction conversion rate of the methane oxidation reaction are both high, and the preparation cost of the catalyst is relatively low. Simultaneously in order to promote response speed and reduce the energy consumption of heating process, the device that this embodiment adopted has chooseed induction heating as the heating method of methane oxidation reactor for use. Meanwhile, in order to further reduce energy consumption, the tail end of the methane oxidation reactor is provided with a heat exchanger, and the discharged high-temperature product gas is used for preheating the inlet gas.

Closely combine above characteristics and the specific operating mode demand, this embodiment pertinence has provided a colliery wind and has discharged gas low concentration methane oxidation desorption system, wherein not only realizes the methane oxidation reaction of low energy consumption, high response speed through the design of methane oxidation catalyst, has realized CO through the carbon capture reactor moreover₂And (5) a capturing process. The equipment can realize a stable, low-energy-consumption and high-efficiency methane oxidation removal process under the conditions of low cost and compact equipment. As shown in fig. 1, the system includes functional components such as an induced draft dust collector 1, a methane oxidation reactor 2, a carbon capture reactor 3, a calcium-based adsorbent feeder 4, and a heat exchanger 5, which will be explained one by one.

The induced air dust removal device 1 is connected with the methane oxidation reactor 2, and the induced air dust removal device 1 filters and removes dust from air exhaust gas, and then the air exhaust gas is sent into the methane oxidation reactor 2 to have oxidation reaction with a catalyst.

The methane oxidation reactor 2 is filled with a methane oxidation catalyst, when the temperature of the methane oxidation reactor is raised to a first specified temperature under the condition of induction heating, the methane oxidation reaction is carried out on the surface of the catalyst by the air exhaust gas fed by the induced air dust removal device 1, and H is generated₂O and CO₂To produce a gas. The temperature of the generated gas is reduced by a heat exchanger 5 at the tail end of the methane oxidation reactor 2, and the heat exchanger 5 sends heat back to the inlet of the methane oxidation reactor 2 to preheat inlet gas.

CO-CONTAINING FORMED BY METHANE OXIDATION REACTOR 2₂The gas enters a carbon capture reactor 3, CO₂Reacts with the calcium adsorbent in the carbon capture reactor 3 and is captured in the calcium adsorbent. And simultaneously, the gas flow subjected to methane oxidation removal and carbon capture can be discharged into the atmosphere.

The calcium sorbent feeder 4 is connected to the carbon capture reactor 3, and the calcium sorbent feeder 4 continuously feeds and recovers the sorbent after the reaction during the carbon capture process, thereby maintaining a sufficient amount of calcium-based sorbent in the bed of the carbon capture reactor 3 for the carbon capture reaction.

In the embodiment, the methane oxidation reaction and the carbon capture process are coupled, the low-energy-consumption oxidation reaction is realized in an induction heating mode, and the carbon capture is performed by applying a calcium-based absorbent. The method not only can give full play to the high performance of the nano copper-based methane oxidation catalyst, but also can realize low-cost carbon dioxide capture, and considers the optimal configuration of energy utilization rate, energy consumption and material utilization on the whole.

The methane oxidation catalyst comprises nano-belt CuO, 316 stainless steel particles and cordierite honeycomb ceramic, wherein the nano-belt CuO, the 316 stainless steel particles and the cordierite honeycomb ceramic are sequentially 10-20% by mass, 10-30% by mass and 50-80% by mass of a cordierite honeycomb ceramic carrier; the nano copper oxide is used as an oxidation reaction catalyst, the stainless steel particles are used as heating bodies, and the cordierite honeycomb ceramic is used as a carrier material.

Example 2:

as shown in fig. 2, the preparation process of the catalyst in example 1 includes the following steps:

first, Cu (NO) is disposed₃)₂The solution, ammonia water and NaOH solution with the molar concentrations of 0.5mmol/L, 0.15mol/L and 1mol/L respectively are added into Cu (NO) under the conditions of 50 ℃ temperature and stirring₃)₂Slowly dripping ammonia water, ammonia water and Cu (NO) into the solution₃)₂Volume ratio control site of solution 3: and 10, dropwise adding an NaOH solution into the mixed solution until the pH value of the mixed solution is 9-10, thus obtaining a blue suspended precursor solution, finally carrying out 5-time centrifugal precipitation, wherein the centrifugal rotation speed is 8000rpm, the centrifugal time is 5min, removing supernatant after each centrifugation, and supplementing deionized water according to the same volume.

And then, taking the blue suspension precursor solution, obtaining blue precipitate slurry through centrifugal precipitation, transferring the blue precipitate slurry into a reaction kettle, heating to 130 ℃ at the speed of 5 ℃/min, and preserving heat for 10 hours. And after cooling, performing centrifugal separation on the generated black slurry, wherein the centrifugal rotation speed is 10000rpm, the centrifugal time is 10min, and drying is performed at 80 ℃ for 24h to obtain black powder which is the nano copper oxide catalyst.

Then, putting the 316 stainless steel particles of 200-300 meshes into 1mol/L polyethylene glycol solution, soaking the cordierite honeycomb ceramic for 2 hours under the stirring condition, taking out the cordierite honeycomb ceramic, drying and aging the cordierite honeycomb ceramic at the temperature of 105-130 ℃ for 12 hours, and then performing high-temperature calcination treatment in several times, wherein the calcination temperature is 400 ℃ and the calcination time is 3 hours;

and then mixing the black catalyst powder with absolute ethyl alcohol at the concentration of 0.1-0.3 mol/L to form catalyst slurry, putting the prepared honeycomb ceramic into the catalyst slurry for dipping treatment under the stirring condition, and then drying again to obtain the required oxygen carrier product.

Through the conception, on one hand, the methane oxidation removal reaction is realized by taking the nano copper oxide as the core of the catalyst, the 316 stainless steel particles are mainly used in the induction heating process to heat the catalyst at high response speed, and the honeycomb ceramic is used as a carrier material to support the catalyst and the stainless steel particles. The honeycomb ceramic catalyst can realize a methane oxidation reaction process with low cost, high energy utilization rate and environmental friendliness under the conditions of low energy consumption, quick start and high dynamic response, and the preparation process is simple and easy to realize industrialization.

As shown in fig. 3, a process for producing the carbon trapping absorbent (calcium-based absorbent) in example 1 was designed; the preparation process specifically comprises the following steps:

(a) take Ca (OH)₂Mixing the powder and a polyethylene glycol aqueous solution (the concentration of polyethylene glycol is 1-2 mol/L) at normal temperature to form a viscous block, and then putting the viscous block into an extruder to extrude the viscous block to form a strip-shaped precursor product with the diameter of about 2-3 mm.

(b) And (b) putting the precursor formed by extrusion in the step (a) into a rounding machine, controlling the rotating speed at 60rpm, and rotating for 60min, wherein the strip-shaped precursor forms a particle product with the thickness of about 2-3 mm under the action of force through the rotating process.

(c) And (c) drying the particle product formed in the step (b) at the temperature of 80-105 ℃ for 24 hours, and then calcining the particle product at the temperature of 700 ℃ for 3 hours to obtain the required calcium-based absorbent.

Example 3:

the specific working process of the methane oxidation removal system is as follows:

when the system is started, the methane oxidation reactor heats the catalyst through induction heating, and when the preset temperature is reached, the induced air dust removal device sucks air exhaust gas and removes dust, and then the air exhaust gas is introduced into the methane oxidation reactor.

When the methane oxidation reactor is heated to reach 400 ℃ by induction heating, the methane is introduced into the methane oxidation reactor through the air exhaust gas of the induced air dust removal device and the methane oxidation reaction is carried out to generate CO₂And H₂At a reaction temperature of 400 ℃, methane can be converted to nearly 100%. Meanwhile, gas after reaction is cooled through a heat exchanger, and the heat exchanger heats the inlet gas at the same time to reduce energy consumption.

Introducing the product gas in the methane oxidation reactor into a carbon capture reactor, and reacting with calcium adsorbentReaction takes place, CO in the gas₂Is captured by the calcium adsorbent.

The calcium absorbent feeder is connected with the carbon capture reactor, and the calcium absorbent feeder continuously feeds materials and recovers absorbent after reaction in the carbon capture process, so that sufficient calcium-based absorbent is kept in a bed layer of the carbon capture reactor for carbon capture reaction.