Use of a zirconium hydrophosphate catalyst in carbon dioxide desorption

Abstract

The application relates to an application of a zirconium hydrogen phosphate (ZrHP) catalyst in carbon dioxide (CO2) desorption. Specifically comprising the following steps: mixing the zirconium hydrogen phosphate catalyst with a CO2-rich amine solution, and carrying out catalytic desorption under heating conditions to realize efficient regeneration of the amine solution. The zirconium hydrogen phosphate catalyst can significantly improve the desorption rate of CO2 and effectively reduce the energy consumption of the desorption process due to its rich acid sites and strong acid characteristics. The application provides an efficient and energy-saving solution for the field of CO2 capture and desorption, and has good industrial application potential.

Description

TECHNICAL FIELD

[0001] The application relates to the field of carbon dioxide capture and separation technology, in particular to application of a zirconium hydrogen phosphate catalyst in carbon dioxide desorption. BACKGROUND

[0002] Global warming is becoming increasingly serious, and carbon dioxide (CO2) as a major greenhouse gas, its emission control and capture technology is concerned. Fossil fuel combustion is one of the main sources of CO2 emission, leading to the concentration rising in the atmosphere, aggravating climate change. Therefore, it is particularly important to develop efficient CO2 capture technology. The traditional CO2 capture method mainly includes physical adsorption and chemical absorption, and the amine absorption method assisted by catalyst is widely used due to high capture efficiency.

[0003] In the related art, under high temperature and alkaline environment, the activity site of the catalyst has a high deactivation rate and poor cycle stability, and the main reasons may include that the acid sites on the surface of the catalyst are covered by amine molecules or byproducts in the capture process, or that the structure is easily damaged by multiple thermal cycles. In addition, the regeneration process of the catalyst often needs high-temperature calcination and other processes, which is complex and time-consuming, and further reduces the continuous operation of CO2 capture. SUMMARY

[0004] The application provides application of a zirconium hydrogen phosphate catalyst in carbon dioxide desorption, the first purpose aims to at least solve the problem of poor cycle stability of the catalyst in the related art, and the second purpose aims to at least solve the problem of complex regeneration process.

[0005] The application provides application of a zirconium hydrogen phosphate catalyst in carbon dioxide desorption, including the following steps:

[0006] The zirconium hydrogen phosphate catalyst and the amine solution containing carbon dioxide are mixed and heated to obtain a mixture after carbon dioxide desorption.

[0007] According to an embodiment of one aspect of the application, the application further includes: centrifuging the mixture to obtain the regenerated zirconium hydrogen phosphate catalyst.

[0008] According to an embodiment of one aspect of the application, the mass ratio of the zirconium hydrogen phosphate catalyst to the amine solution is (0-0.3):1.

[0009] According to an embodiment of one aspect of the application, in the amine solution, the amine is at least one of monoethanolamine, diethanolamine, triethanolamine, methyldiethanolamine, diethyl ethanolamine, piperazine, diisopropanolamine and aminoethanol.

[0010] According to an embodiment of one aspect of the application, the carbon dioxide loading in the amine solution is 0.2-0.6 mol CO2 / mol amine.

[0011] According to an embodiment of one aspect of the present application, the zirconium hydrogen phosphate catalyst is in a layered structure.

[0012] According to an embodiment of one aspect of the present application, the 002 crystal face orientation ratio of the zirconium hydrogen phosphate catalyst is 45% to 80%.

[0013] According to an embodiment of one aspect of the present application, the heating temperature is 80 to 130 DEG C during the mixing and heating.

[0014] According to an embodiment of one aspect of the present application, the centrifugal speed is 6000 to 10000 rpm during the centrifugal separation.

[0015] According to an embodiment of one aspect of the present application, the centrifugal time is 8 to 20 minutes.

[0016] Compared with the prior art, the present application has at least the following beneficial effects:

[0017] 1. The zirconium hydrogen phosphate catalyst is used for carbon dioxide desorption in the embodiments of the present application. The zirconium hydrogen phosphate (ZrHP) catalyst has abundant acid sites and obvious strong acid characteristics, which can improve the desorption rate of amine solution in the CO2 desorption process and reduce the desorption energy consumption.

[0018] 2. The ZrHP catalyst used in the embodiments of the present application has excellent cycle stability. After being used for multiple cycles, the catalytic activity of the ZrHP catalyst is not less than 75%, and the deactivation rate of the active site is low. The ZrHP catalyst exhibits excellent cycle stability in the desorption process.

[0019] 3. The zirconium hydrogen phosphate catalyst provided in the embodiments of the present application is easy to obtain, low in cost and simple in regeneration operation. The catalyst is regenerated by centrifugation for the next CO2 desorption cycle, avoiding complex steps such as high-energy drying and calcination, optimizing the regeneration process, requiring less time and significantly reducing the regeneration energy consumption, and meeting the needs of continuous industrial operation. BRIEF DESCRIPTION OF DRAWINGS

[0020] The features, advantages and technical effects of the exemplary embodiments of the present application will be described below with reference to the accompanying drawings.

[0021] Figure 1 The X-ray diffraction pattern of the zirconium hydrogen phosphate catalyst provided in the embodiments of the present application.

[0022] Figure 2 The scanning electron microscope image of the zirconium hydrogen phosphate catalyst provided in the embodiments of the present application.

[0023] Figure 3 The NH3-TPD pattern of the zirconium hydrogen phosphate catalyst provided in the embodiments of the present application.

[0024] Figure 4 The CO2 desorption diagrams are provided for different embodiments of this application.

[0025] Figure 5 Energy consumption diagrams for catalytic desorption in different embodiments provided in this application.

[0026] Figure 6 The graph shows the instantaneous percentage increase in CO2 desorption rate and the percentage increase in cumulative CO2 desorption amount in different embodiments provided in this application.

[0027] Figure 7 Performance diagram of repeated use of Embodiment 4 provided in this application.

[0028] Figure 8 The catalytic desorption performance of the ZrHP-4 catalyst provided in this application at different temperatures is shown in the figure.

[0029] Figure 9 The diagram shows the catalytic desorption performance of the ZrHP-4 catalyst provided in this application in different amine solutions. Detailed Implementation

[0030] To make the objectives, technical solutions, and beneficial effects of this invention clearer, the invention will be further described in detail below with reference to the accompanying drawings and embodiments. It should be understood that the drawings and embodiments described in this specification are merely for explaining the invention and are not intended to limit the invention.

[0031] For simplicity, this paper only explicitly discloses some numerical ranges. However, any lower limit can be combined with any upper limit to form an unspecified range; and any lower limit can be combined with other lower limits to form an unspecified range, just as any upper limit can be combined with any other upper limit to form an unspecified range. Furthermore, although not explicitly stated, every point or individual value between the endpoints of a range is included within that range. Therefore, each point or individual value can be used as its own lower or upper limit, combined with any other point or individual value, or combined with other lower or upper limits to form an unspecified range.

[0032] In this description, it should be noted that, unless otherwise stated, "above" and "below" include the stated number, "multiple" in "one or more" means two or more, and "more than" in "one or more" means two or more.

[0033] The above description of the invention is not intended to describe every disclosed embodiment or implementation of the invention. Instead, the following description provides more specific examples of exemplary embodiments. Throughout this application, guidance is provided through a series of embodiments that can be used in various combinations. The examples listed are representative only and should not be construed as exhaustive.

[0034] Embodiments of this application provide an application of a zirconium hydrogen phosphate catalyst in carbon dioxide desorption, comprising the following steps:

[0035] The zirconium hydrogen phosphate catalyst and an amine solution containing carbon dioxide were mixed and heated to obtain a mixture after carbon dioxide desorption.

[0036] According to the embodiments of this application, zirconium hydrogen phosphate (ZrHP) catalyst is used for carbon dioxide desorption. The ZrHP catalyst exhibits ion exchange characteristics similar to ion exchange resins, as well as shape-selective adsorption and catalytic capabilities similar to zeolites. In particular, it possesses abundant acidic sites and significant strong acid characteristics, which can enhance the desorption rate of amine solutions during CO2 desorption and reduce desorption energy consumption. The ZrHP catalyst demonstrates excellent cycle stability; after multiple cycles, its catalytic activity remains at least 75%, with a low active site deactivation rate, exhibiting excellent cycle stability during desorption.

[0037] In some embodiments, the application further includes centrifuging the mixture to obtain a regenerated zirconium hydrogen phosphate catalyst.

[0038] According to the embodiments of this application, the zirconium hydrogen phosphate catalyst is easy to obtain, inexpensive, and simple to regenerate. The catalyst can be directly regenerated by centrifugation for use in the next CO2 desorption cycle, avoiding complex steps such as high-energy-consuming drying and calcination, optimizing the regeneration process, requiring less time, significantly reducing regeneration energy consumption, and better meeting the needs of continuous industrial operation.

[0039] In some embodiments, the mass ratio of zirconium hydrogen phosphate catalyst to amine solution is (0-0.3):1, and is not 0.

[0040] According to embodiments of this application, a suitable mass ratio of zirconium hydrogen phosphate catalyst to amine solution can greatly enhance the catalytic efficiency of the zirconium hydrogen phosphate catalyst.

[0041] In some embodiments, the amine in the amine solution is selected from at least one of monoethanolamine, diethanolamine, triethanolamine, methyldiethanolamine, diethylethanolamine, piperazine, diisopropanolamine, and aminoethanol.

[0042] According to the embodiments of this application, the zirconium hydrogen phosphate catalyst has wide applicability when applied to carbon dioxide desorption and exhibits good catalytic performance in various monoamine or mixed amine solutions.

[0043] In some embodiments, the carbon dioxide loading in the amine solution is 0.2-0.6 mol CO2 / mol amine.

[0044] According to the embodiments of the present application, the zirconium hydrogen phosphate catalyst is suitable for the CO2-rich amine solution and enhances the desorption of the CO2-rich amine solution.

[0045] In some embodiments, the zirconium hydrogen phosphate catalyst is a layered structure.

[0046] According to the embodiments of the present application, the zirconium hydrogen phosphate catalyst is a layered structure, which has good thermal stability and chemical stability and is suitable for applications requiring high stability and corrosion resistance.

[0047] In some embodiments, the 002 crystal plane orientation ratio of the zirconium hydrogen phosphate catalyst is 45%-80%.

[0048] The 002 crystal plane ratio is commonly found in hexagonal or cubic crystal materials, which refers to the ratio or relative intensity of a specific crystal plane (such as the 002 crystal plane) in all crystal planes in a crystal material, which is usually determined by X-ray diffraction (XRD) analysis. The 002 crystal plane ratio is an important parameter for characterizing the structure of a crystal material, and different crystal plane ratios affect the thermal stability, chemical stability and catalytic performance of the catalyst.

[0049] According to the embodiments of the present application, within a suitable range of 002 crystal plane orientation ratio, the zirconium hydrogen phosphate catalyst maintains stable and excellent catalytic performance, and the higher the 002 crystal plane orientation ratio, the better the catalytic performance.

[0050] In some embodiments, the heating temperature is 80-130°C when mixed heating.

[0051] According to the embodiments of the present application, the zirconium hydrogen phosphate catalyst requires a lower heating temperature while maintaining the same catalytic performance, further reducing the energy consumption required during desorption.

[0052] In some embodiments, the centrifugal speed is 6000-10000 revolutions per minute when centrifuging.

[0053] In some embodiments, the centrifugation time is 8-20 minutes.

[0054] According to the embodiments of the present application, solid-liquid separation can be completed by simple centrifugation, so that the zirconium hydrogen phosphate catalyst can be quickly regenerated without complicated steps such as drying or high-temperature calcination, and the regeneration time is short, the steps are simple, and the energy consumption is reduced.

[0055] Embodiments

[0056] The present application is further described in the following examples that are intended to be illustrative only, as various modifications and changes in the application disclosed herein will become apparent to those skilled in the art. Unless otherwise indicated, all parts, percentages, and ratios reported herein are on a weight basis, and all reagents used in the examples were commercially available or were synthesized using standard techniques known to one skilled in the art, and used without further purification, and the equipment used in the examples was commercially available.

[0057] The following examples provide four kinds of zirconium hydrogen phosphate catalysts, which are purchased from Tianjin Baima Technology Co., Ltd., Jingmen Dongxin Biological Technology Co., Ltd., Mianzhu Yaolong Chemical Co., Ltd. and Aladdin Biochemical Technology Co., Ltd., respectively, and are named ZrHP-1, ZrHP-2, ZrHP-3 and ZrHP-4.

[0058] Catalyst characterization: The above catalysts were characterized by X-ray diffraction (XRD), scanning electron microscopy (SEM) and ammonia temperature programmed desorption (NH3-TPD) methods, respectively.

[0059] As shown in Figures 1 to 3 , wherein, Figure 1 is the X-ray diffraction pattern of the zirconium hydrogen phosphate catalyst provided in the embodiments of the present application. Figure 2 is the scanning electron microscope image of the zirconium hydrogen phosphate catalyst provided in the embodiments of the present application. Figure 3 is the NH3-TPD spectrum of the zirconium hydrogen phosphate catalyst provided in the embodiments of the present application.

[0060] It should be noted that Figure 3 The related catalyst HZSM-5 catalyst as a reference control is also included in the embodiments of the present application. HZSM-5 catalyst is a solid acid catalyst with strong acidity and ZSM-5 molecular sieve as carrier, which is widely used at present.

[0061] Figure 1 The material composition and crystal structure of the four kinds of zirconium hydrogen phosphate catalysts are shown, and the data are shown in Table 1. Figure 2 The structure of the zirconium hydrogen phosphate catalyst is shown. Figure 3 The catalytic performance of the zirconium hydrogen phosphate catalyst is shown, and the data are shown in Table 2.

[0062] Table 1 Crystal plane composition of ZrHP catalyst

[0063]

[0064] Table 2 Number of acid sites of catalyst

[0065]

[0066] FromFigure 1 As shown in Table 1, the orientation of the 002 crystal plane accounts for the majority in the crystal structure of the zirconium hydrogen phosphate catalyst. Figure 2 As shown in Table 1, the orientation of the 002 crystal plane accounts for the majority in the crystal structure of the zirconium hydrogen phosphate catalyst. Figure 3 The desorption peak in the middle indicates that there are acidic sites on the surface of the material, and the strength and quantity of the acidic sites directly affect the catalytic activity of the zirconium hydrogen phosphate catalyst. The higher the temperature of the desorption peak, the greater the strength of the acidic sites; the larger the area of the desorption peak, the more the acidic sites; the more the number of desorption peaks, the more the different strength of the acidic sites. Figure 3 As shown in Table 2, the zirconium hydrogen phosphate catalyst not only has weak acid and medium strong acid sites, but also exhibits obvious strong acid characteristics.

[0067] The following examples all use a batch CO2 desorption device as the CO2 desorption system. The batch CO2 desorption device includes a reactor with a heating jacket, a stirring device in the reactor, and is connected with a mass flow meter, a CO2 infrared analyzer and a power meter. The mass flow meter controls the flow of the outlet mixed gas (N2 and desorbed CO2), the CO2 infrared analyzer monitors the concentration of CO2 in the mixed gas in real time, and the power meter records the energy consumption of the system during the whole reaction process.

[0068] The desorption time is determined according to actual needs, such as the heating mode can be selected as oil bath or water bath, so as to determine the corresponding desorption time.

[0069] Example 1

[0070] 100 milliliters of amine solution and ZrHP-1 catalyst were added to the reaction, the amine solution was 5M monoethanolamine (MEA) solution loaded with 0.5mol CO2 / mol MEA, and the mass ratio of ZrHP-1 catalyst to amine solution was 1.25%:1. The stirring device was started, nitrogen was introduced to replace the air in the system; the heating jacket was started, and the heating temperature was gradually increased to 90℃, and desorption was carried out for 60 minutes to obtain a mixture after desorption of carbon dioxide. During the period, the temperature was monitored in real time by a temperature probe and kept stable, and the CO2 desorption rate and energy consumption data were recorded and analyzed. Taking 1000s as an example, the CO2 desorption performance was calculated, and the calculation results are shown in Table 3. The CO2 desorption amount is shown in Table 3, and the energy consumption of catalytic desorption is shown in Table 3. Figure 4 Figure 5

[0071] Example 2

[0072] The difference between Example 2 and Example 1 is only that the ZrHP-1 catalyst is replaced by ZrHP-2 catalyst. The calculation results of the CO2 desorption performance are shown in Table 3. The CO2 desorption amount is shown in Table 3, and the energy consumption of catalytic desorption is shown in Table 3. Figure 4 Figure 5

[0073] Example 3​​​​

[0074] Example 3 differs from Example 1 only in that the ZrHP-1 catalyst is replaced by the ZrHP-3 catalyst. The calculated results of the CO2 desorption performance are shown in Table 3. The amount of CO2 desorbed is shown in Figure 4 , and the energy consumption of the catalytic desorption is shown in Figure 5 .

[0075] Example 4

[0076] Example 4 differs from Example 1 only in that the ZrHP-1 catalyst is replaced by the ZrHP-4 catalyst. The calculated results of the CO2 desorption performance are shown in Table 3. The amount of CO2 desorbed is shown in Figure 4 , and the energy consumption of the catalytic desorption is shown in Figure 5 .

[0077] After the completion of desorption, the mixture was separated by centrifugation to achieve the regeneration of the ZrHP-4 catalyst, and 10 desorption experiments were performed to verify the stability and repeatability of its cyclic use, and the results are shown in Figure 7 .

[0078] Example 5

[0079] Example 5 differs from Example 4 only in that the heating temperature is 86°C. The results of the catalytic desorption performance are shown in Figure 8 .

[0080] Example 6

[0081] Example 6 differs from Example 4 only in that the heating temperature is 94°C. The results of the catalytic desorption performance are shown in Figure 8 .

[0082] Example 7

[0083] Example 7 differs from Example 4 only in that the heating temperature is 98°C. The results of the catalytic desorption performance are shown in Figure 8 .

[0084] Example 8

[0085] Example 8 differs from Example 4 only in that the heating temperature is 110°C. The results of the catalytic desorption performance are shown in Figure 8 .

[0086] Example 9

[0087] Example 9 differs from Example 4 only in that the monoethanolamine (MEA) solution is replaced by a 3-aminopropanol solution (3AP, 0.57 mol CO2 / mol N). The results of the catalytic desorption performance are shown in Figure 9 .

[0088] Example 10

[0089] Example 10 differs from Example 4 only in that the monoethanolamine (MEA) solution is replaced by a N,N-dimethylethanolamine solution (DMEA, 0.40 mol CO2 / mol N). The catalytic desorption performance results are shown in Table 3. Figure 9

[0090] Example 11

[0091] Example 11 differs from Example 4 only in that the monoethanolamine (MEA) solution is replaced by a N-methyl-2-hydroxyethylamine solution (MAE, 0.69 mol CO2 / mol N). The catalytic desorption performance results are shown in Table 3. Figure 9

[0092] Example 12

[0093] Example 12 differs from Example 4 only in that the monoethanolamine (MEA) solution is replaced by a diethanolamine solution (DEA, 0.61 mol CO2 / mol N). The catalytic desorption performance results are shown in Table 3. Figure 9

[0094] Blank

[0095] Blank differs from Example 1 only in that no catalyst is added, serving as a blank control. The calculated results of CO2 desorption performance are shown in Table 3. The CO2 desorption amount is shown in Table 3, and the energy consumption of catalytic desorption is shown in Table 3. Figure 4 Figure 5

[0096] Without adding a catalyst, the desorption reaction rate reaches a peak value (27.87 x 10 -5 mol s -1 L -1 ) at 1000 s, and the CO2 desorption amount at this time is 10.43 mmol, and the relative energy consumption is set to 100%.

[0097] Reference 2

[0098] Reference 2 differs from Example 1 only in that the ZrHP-1 catalyst is replaced by the same mass of HZSM-5 catalyst, serving as a reference control. The calculated results of CO2 desorption performance are shown in Table 3. The CO2 desorption amount is shown in Table 3, and the energy consumption of catalytic desorption is shown in Table 3. Figure 4 Figure 5

[0099] Reference 3

[0100] Reference 3 differs from Reference 1 only in that the heating temperature is 86°C. The catalytic desorption performance results are shown in Table 3. Figure 8 ​​​​​​​shown.

[0101] Comparative Example 4

[0102] Comparative Example 4 differs from Comparative Example 1 only in that the heating temperature was 94 °C. The catalytic desorption performance results are shown in Table 1. Figure 8

[0103] Comparative Example 5

[0104] Comparative Example 5 differs from Comparative Example 1 only in that the heating temperature was 98 °C. The catalytic desorption performance results are shown in Table 1. Figure 8

[0105] Comparative Example 6

[0106] Comparative Example 6 differs from Comparative Example 1 only in that the heating temperature was 110 °C. The catalytic desorption performance results are shown in Table 1. Figure 8

[0107] Comparative Example 7

[0108] Comparative Example 7 differs from Comparative Example 1 only in that the monoethanolamine (MEA) solution was replaced with a 3-aminopropanol solution (3AP, 0.57 mol CO2 / mol N). The catalytic desorption performance results are shown in Table 1. Figure 9

[0109] Comparative Example 8

[0110] Comparative Example 8 differs from Comparative Example 1 only in that the monoethanolamine (MEA) solution was replaced with a N,N-dimethylethanolamine solution (DMEA, 0.40 mol CO2 / mol N). The catalytic desorption performance results are shown in Table 1. Figure 9

[0111] Comparative Example 9

[0112] Comparative Example 9 differs from Comparative Example 1 only in that the monoethanolamine (MEA) solution was replaced with a N-methyl-2-hydroxyethylamine solution (MAE, 0.69 mol CO2 / mol N). The catalytic desorption performance results are shown in Table 1. Figure 9

[0113] Comparative Example 10

[0114] Comparative Example 10 differs from Comparative Example 1 only in that the monoethanolamine (MEA) solution was replaced with a diethanolamine solution (DEA, 0.61 mol CO2 / mol N). The catalytic desorption performance results are shown in Table 1. Figure 9

[0115] Table 3 CO2 desorption performance at 1000 s

[0116] ​​​​​​​

[0117] In terms of CO2 desorption amount, from Table 3 and Figure 4 It can be seen that, compared with Comparative Example 1 as a blank control, the CO2 desorption amount of Example 2 as a reference control increased only by 23% after adding the HZSM-5 catalyst; while the CO2 desorption amount of Examples 1 to 4, especially Example 4 with the added ZrHP-4 catalyst, was significantly improved by 94%.

[0118] In terms of energy consumption reduction, from Table 3 and Figure 5 It can be seen that, compared with Comparative Example 1 as a blank control (the relative energy consumption is set to 100%), the energy consumption of Example 2 as a reference control was reduced only by 19% after adding the HZSM-5 catalyst; while the energy consumption of Examples 1 to 4, especially Example 4 with the ZrHP-4 catalyst, was reduced by up to 48.48%.

[0119] The results of significant improvement in CO2 desorption amount and significant reduction in energy consumption are mainly due to the rich number and strength of acidic sites of the ZrHP catalyst. As can be seen from Table 2, the ZrHP catalyst not only has weak acid and medium-strong acid sites, but also exhibits obvious strong acid characteristics, so that the total acid amount is much higher than that of the HZSM-5 catalyst. These high-acid sites effectively promote the breaking of the C-N bond in the CO2 desorption process, thereby accelerating the desorption reaction. The ZrHP catalyst achieves efficient desorption and reduces energy consumption, and its performance is superior to most existing solid acid catalysts.

[0120] Please refer to Figure 6 , Figure 6 the CO2 desorption rate instant percentage increase and the CO2 cumulative desorption amount percentage increase graphs provided in the different embodiments of the present application.

[0121] In terms of CO2 desorption rate instant percentage increase and CO2 cumulative desorption amount percentage increase, from Figure 6 It can be seen that, compared with Comparative Example 1 as a blank control, Example 4 with the ZrHP-4 catalyst, the instantaneous CO2 desorption rate was increased by as much as 526%, while Comparative Example 2 with the HZSM-5 catalyst, the instantaneous CO2 desorption rate was only increased by 70%; Example 4 with the ZrHP-4 catalyst, the CO2 cumulative desorption amount was increased by as much as 394%, while Comparative Example 2 with the HZSM-5 catalyst, the CO2 cumulative desorption amount was only increased by 57%, which further illustrates the potential of ZrHP catalyst in desorption of CO2-rich amine solution.

[0122] In terms of stability and repeatability of catalyst recycling, from Figure 7It can be seen that after the first cycle and ten cycles, the CO2 desorption reaction rate remained almost unchanged, effectively shortening the reaction time. This indicates that the catalyst has excellent cycle stability and significantly improves the regeneration efficiency of CO2-rich amine solutions. This stability mainly stems from the good thermal stability and catalytic activity of the ZrHP-4 catalyst, ensuring that it maintains its structure and performance through multiple cycles. It also suggests that there may be little or no byproduct generation during desorption, the structure of the ZrHP catalyst is rarely or almost undamaged, and the deactivation rate of the catalyst active sites is low, meaning that the ZrHP catalyst has anti-poisoning ability. Compared with the MEA solution without catalyst, after ten cycles, the relative heat load of the catalyst decreased by about 30%, significantly improving energy efficiency.

[0123] ZrHP-4 catalyst exhibits different catalytic performances at different heating temperatures. Figure 8 As can be seen, compared to Comparative Example 4 without a catalyst at 94℃, Example 4 using the ZrHP-4 catalyst at 90℃ showed a 14.3% higher CO2 desorption capacity, indicating that the ZrHP-4 catalyst significantly improves desorption efficiency at lower temperatures, thereby effectively reducing energy consumption. Furthermore, at 110℃, Example 8 using the ZrHP-4 catalyst showed a calculated energy consumption reduction of 25.1%, further demonstrating its excellent catalytic performance under high-temperature conditions, making it highly suitable for alkaline operations at high temperatures.

[0124] ZrHP-4 catalysts exhibit varying catalytic performance in different amine solutions. Figure 9 It can be seen that, compared with the non-catalytic conditions of Comparative Examples 7-10 (serving as a blank control), the CO2 desorption rates of the four amine solutions in Examples 9-12 were significantly higher under the catalytic conditions with the addition of ZrHP-4 catalyst than under the non-catalytic conditions, especially Example 10 using DMEA amine solution. Specifically, under non-catalytic conditions, the reaction rate constant of DMEA in Comparative Example 8 was 4.47 × 10⁻⁶. -5 s -1 Under catalytic conditions, the reaction rate constant of DMEA in Example 10 increased to 7.22 × 10⁻⁶. -5 s -1 The regeneration rate increased by 61.52%, while energy consumption decreased by 22.23%. These results further demonstrate that the ZrHP-4 catalyst effectively reduces energy consumption while improving the regeneration rate of different amine solutions (such as 3AP, DMEA, MAE, and DEA). These performance improvements highlight the broad application potential of this catalyst in CO2 capture technology, warranting further research and application, and laying a solid foundation for the future development of CO2 capture technology.

[0125] Although the present application has been described with reference to preferred embodiments, it is to be understood that various modifications can change the scope of the present application to the full extent that equivalents, under the doctrine of equivalents to the full extent indicated by the doctrine of equivalents, are permissible. Furthermore, it is to be understood that the scope of the present application is not limited to the particular embodiments disclosed herein but covers modifications obvious to those skilled in the art within the scope of the present application.

Claims

1. The application of a zirconium hydrogen phosphate catalyst in carbon dioxide desorption, characterized in that, Includes the following steps: The zirconium hydrogen phosphate catalyst and the CO2-rich amine solution were mixed and heated to obtain a mixture after CO2 desorption.

2. The application of the zirconium hydrogen phosphate catalyst according to claim 1 in carbon dioxide desorption, characterized in that, The application also includes centrifuging the mixture to obtain a regenerated zirconium hydrogen phosphate catalyst.

3. The application of the zirconium hydrogen phosphate catalyst according to claim 1 in carbon dioxide desorption, characterized in that, The mass ratio of the zirconium hydrogen phosphate catalyst to the amine solution is (0-0.3):

1.

4. The application of the zirconium hydrogen phosphate catalyst according to claim 1 in carbon dioxide desorption, characterized in that, In the amine solution, the amine is selected from at least one of monoethanolamine, diethanolamine, triethanolamine, methyldiethanolamine, diethylethanolamine, piperazine, diisopropanolamine, and aminoethanol.

5. The application of the zirconium hydrogen phosphate catalyst according to claim 1 in carbon dioxide desorption, characterized in that, The CO2 loading in the amine solution is 0.2–0.6 mol CO2 / mol amine.

6. The application of the zirconium hydrogen phosphate catalyst according to claim 1 in carbon dioxide desorption, characterized in that, The zirconium hydrogen phosphate catalyst has a layered structure.

7. The application of the zirconium hydrogen phosphate catalyst according to claim 6 in carbon dioxide desorption, characterized in that, The 002 crystal plane orientation ratio of the zirconium hydrogen phosphate catalyst is 45% to 80%.

8. The application of the zirconium hydrogen phosphate catalyst according to claim 1 in carbon dioxide desorption, characterized in that, When heating with a mixture, the heating temperature is 80–130℃.

9. The application of the zirconium hydrogen phosphate catalyst according to claim 2 in carbon dioxide desorption, characterized in that, During centrifugation, the centrifugation speed is 6000–10000 rpm.

10. The application of the zirconium hydrogen phosphate catalyst according to claim 9 in carbon dioxide desorption, characterized in that, Centrifugation time is 8 to 20 minutes.

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