V2O5-CeO2 / SFCC-PG catalysis / adsorbent and preparation method and application thereof

Abstract

The invention provides a V2O5-CeO2 / SFCC-PG catalysis / adsorbent and a preparation method and application thereof, and belongs to the technical field of solid waste resource utilization and air pollution control, the catalysis / adsorbent provided by the invention comprises an SFCC-PG (waste FCC catalyst-attapulgite) carrier and V2O5 and CeO2 loaded on the surface of the SFCC-PG carrier. The use temperature of the catalyst / adsorbent is 150-250 DEG C, the catalyst / adsorbent is matched with the exhaust gas temperature of a coal-fired power plant, meanwhile, the catalyst / adsorbent has excellent catalysis and adsorption performance, Hg < 0 > can be subjected to catalytic oxidation to generate a Hg < 2 + > compound, the Hg < 2 + > compound is adsorbed on the catalyst / adsorbent, and the Hg < 2 + > compound does not need to be removed through a wet desulphurization device. Results of the embodiment show that the removal rate of the catalyst / adsorbent provided by the invention on Hg < 0 > at 150-250 DEG C is 85% or above.

Description

Technical Field

[0001] The present invention belongs to the technical fields of solid waste resource utilization and air pollution control, and particularly relates to a V 2 O 5 -CeO 2 / SFCC-PG catalyst / adsorbent, its preparation method and application. Background Art

[0002] Coal is the main energy source in China, and its utilization mainly relies on direct combustion. Mercury is one of the harmful heavy metal pollutants released during coal combustion, posing serious and persistent hazards to the ecological environment and human health. The forms of mercury in coal-fired flue gas mainly include gaseous Hg 0 and Hg 2+ as well as Hg p adsorbed on fly ash. Most of the Hg p and Hg 2+ can be removed through the existing dust removal devices and wet flue gas desulfurization devices in power plants. However, due to its high volatility and low solubility in water, Hg 0 is difficult to be removed by the existing power plant pollutant control devices, thus becoming the focus of mercury removal from coal-fired flue gas.

[0003] Currently, for the emission control of Hg 0 in coal-fired flue gas, the main method is to catalytically oxidize Hg 0 into Hg 2+ , and then remove it through the existing power plant pollutant control devices. Currently, the most studied catalyst is the V 2 O 5 -based commercial SCR catalyst, which uses TiO 2 as the carrier and has high oxidation activity towards Hg 0 . However, its operating temperature is relatively high (300 - 450 °C), and its adsorption capacity is very low. It must be combined with the downstream wet flue gas desulfurization device to remove the Hg 0 oxidized to Hg 2+ . Therefore, there is an urgent need for a catalyst / adsorbent with a low operating temperature and excellent catalytic and adsorption properties. Summary of the Invention

[0004] The purpose of the present invention is to provide a V 2 O 5 -CeO 2 / SFCC-PG catalyst / adsorbent, its preparation method and application. The catalyst / adsorbent provided by the present invention has a low operating temperature and excellent catalytic and adsorption properties simultaneously.

[0005] To achieve the above-mentioned invention purpose, the present invention provides the following technical solutions:

[0006] The present invention provides a V 2 O 5 -CeO 2 / SFCC-PG catalyst / adsorbent, comprising an SFCC-PG support and V 2 O 5 and CeO 2 .

[0007] Preferably, the mass ratio of SFCC to PG in the SFCC-PG support is (5-7):(3-5).

[0008] Preferably, the total mass of V 2 O 5 and CeO 2 is 1-10% of the total mass of the V 2 O 5 -CeO 2 / SFCC-PG catalyst / adsorbent.

[0009] Preferably, the mass ratio of V 2 O 5 and CeO 2 is (3-5):(0.5-2).

[0010] The present invention also provides a preparation method of the V 2 O 5 -CeO 2 / SFCC-PG catalyst / adsorbent according to the above technical solution, comprising the following steps:

[0011] (1) Roast the waste FCC catalyst to obtain the activated waste FCC catalyst;

[0012] (2) Mix the activated waste FCC catalyst obtained in step (1) with attapulgite and water, and sequentially perform drying and sieving to obtain the SFCC-PG support;

[0013] (3) Immerse the SFCC-PG support obtained in step (2) in an equal volume of a vanadium source solution, and then sequentially perform static standing, freezing, and heating drying to obtain vanadium source / SFCC-PG;

[0014] (4) Drop the cerium salt solution onto the surface of the vanadium source / SFCC-PG obtained in step (3), and then sequentially perform static standing, freezing, heating drying, and calcination to obtain the V 2 O 5 -CeO 2 / SFCC-PG catalyst / adsorbent.

[0015] Preferably, the calcination temperature in step (1) is 450-530 °C, and the calcination time is 1-3 h.

[0016] Preferably, the particle size of the SFCC-PG support in step (2) is 30-60 mesh.

[0017] Preferably, the vanadium source solution in step (3) is an oxalic acid solution of ammonium metavanadate.

[0018] Preferably, the calcination temperature in step (4) is 450-550 °C, and the calcination time is 2-4 h.

[0019] The present invention also provides the above-mentioned technical solution of V 2 O 5 -CeO 2 / SFCC-PG catalytic / adsorbent or the V 2 O 5 -CeO 2 / SFCC-PG catalytic / adsorbent prepared by the above-mentioned preparation method is used for the application of removing Hg 0 from flue gas.

[0020] The present invention provides a V 2 O 5 -CeO 2 / SFCC-PG catalytic / adsorbent, comprising an SFCC-PG support and V 2 O 5 and CeO 2 supported on the surface of the SFCC-PG support. The use temperature of the catalytic / adsorbent provided by the present invention is 150-250 °C, which matches the flue gas discharge temperature of coal-fired power plants. At the same time, it has excellent catalytic and adsorption properties, and can catalytically oxidize Hg 0 to generate Hg 2+ compounds and adsorb them on the catalytic / adsorbent, without the need to remove them through a wet flue gas desulfurization device. The results of the examples show that the catalytic / adsorbent provided by the present invention has a removal rate of Hg 0 above 85% at 150-250 °C. Detailed implementation manners

[0021] The present invention provides a V 2 O 5 -CeO 2 / SFCC-PG catalytic / adsorbent, comprising an SFCC-PG support and V 2 O 5 and CeO 2 .

[0022] The V 2 O5 -CeO 2 The V

[0023] -CeO

[0024] / SFCC-PG catalytic / adsorbent comprises an SFCC-PG (spent FCC catalyst - attapulgite) support.

[0025] In the present invention, the spent FCC catalyst (SFCC) is preferably a solid waste from a petrochemical plant. The present invention uses the spent FCC catalyst as a support, enabling the resource utilization of solid waste and reducing the cost of the catalytic / adsorbent. 0 Removal rate.

[0026] In the present invention, the attapulgite (PG) is inexpensive and readily available, which can reduce the cost of the catalytic / adsorbent. 2 O 5 -CeO 2 / SFCC-PG catalytic / adsorbent further comprises V 2 O 5 and CeO 2 .

[0027] In the present invention, the total mass of the V 2 O 5 and CeO 2 is preferably 1-10% of the total mass of the V 2 O 5 -CeO 2 / SFCC-PG catalytic / adsorbent. As an embodiment, the total mass of the V 2 O 5 and CeO 2 can be specifically 1%, 2%, 3%, 4%, 5%, 6%, 7%, 8%, 9% or 10% of the total mass of the V 2 O 5 -CeO 2 / SFCC-PG catalytic / adsorbent.

[0028] In the present invention, the V 2 O 5 and CeO 2The mass ratio is preferably (3-5):(0.5-2). As an implementation, the V 2 O 5 and CeO 2 The mass ratio can specifically be 5:1, 3:2 or 5:0.5. In the present invention, the total mass of V 2 O 5 and CeO 2 and the mass ratio of V 2 O 5 and CeO 2 are controlled within the above ranges, which can further improve the catalytic oxidation of the catalyst / adsorbent, thereby further increasing the removal rate of Hg 0 in flue gas.

[0029] The operating temperature of the catalyst / adsorbent provided by the present invention is 150-250 °C, which matches the flue gas discharge temperature of coal-fired power plants. At the same time, it has excellent catalytic and adsorption properties, and can catalytically oxidize Hg 0 to generate Hg 2+ compounds and adsorb them on the catalyst / adsorbent, eliminating the need for removal by a wet flue gas desulfurization device, reducing operating costs, and enabling the resource utilization of solid waste.

[0030] The present invention also provides a preparation method for the V 2 O 5 -CeO 2 / SFCC-PG catalyst / adsorbent described in the above technical solution, including the following steps:

[0031] (1) Roast the waste FCC catalyst to obtain the activated waste FCC catalyst;

[0032] (2) Mix the activated waste FCC catalyst obtained in step (1) with attapulgite and water, and sequentially perform drying and sieving to obtain the SFCC-PG support;

[0033] (3) Impregnate the SFCC-PG support obtained in step (2) with a vanadium source solution in an equal volume manner, and then sequentially perform static standing, freezing, and heating drying to obtain vanadium source / SFCC-PG;

[0034] (4) Drop the cerium salt solution onto the surface of the vanadium source / SFCC-PG obtained in step (3), and then sequentially perform static standing, freezing, heating drying, and calcination to obtain the V 2 O 5 -CeO 2 / SFCC-PG catalyst / adsorbent.

[0035] Unless otherwise specified, the present invention does not have special limitations on the sources of each raw material, and commercially available products well-known to those skilled in the art can be used.

[0036] The waste FCC catalyst of the present invention is calcined to obtain an activated waste FCC catalyst.

[0037] The present invention has no special limitation on the source of the waste FCC catalyst, and the waste FCC catalyst from petrochemical plant solid waste well-known to those skilled in the art can be used. In the embodiments of the present invention, the main components of the waste FCC catalyst include 53% aluminum oxide, 43% silicon dioxide, 2.8% carbon deposition, 0.9% iron oxide, 0.2% cobalt tetroxide, and 0.1% vanadium pentoxide.

[0038] In the present invention, the calcination temperature is preferably 450 - 530 °C. As an implementation manner, the calcination temperature can specifically be 450 °C, 460 °C, 470 °C, 480 °C, 490 °C, 500 °C, 510 °C, 520 °C, or 530 °C.

[0039] In the present invention, the calcination time is preferably 1 - 3 h. As an implementation manner, the calcination time can specifically be 1 h, 1.5 h, 2 h, 2.5 h, or 3 h.

[0040] In the present invention, the calcination is preferably carried out in an oxygen or air atmosphere. In the present invention, the calcination is used to remove the carbon deposition in the waste FCC catalyst. The present invention controls the calcination temperature and time within the above ranges, which can enable the carbon deposition in the waste FCC catalyst to be fully combusted and removed, further increasing the porosity of the waste FCC catalyst, thereby contributing to improving the catalytic and adsorption performance of the catalyst / adsorbent.

[0041] After the calcination is completed, the present invention preferably naturally cools the calcined product to room temperature to obtain an activated waste FCC catalyst.

[0042] After obtaining the activated waste FCC catalyst, the present invention mixes the activated waste FCC catalyst with attapulgite and water, and successively performs drying and sieving to obtain an SFCC - PG support.

[0043] In the present invention, the mass ratio of the activated waste FCC catalyst to attapulgite is preferably (5 - 7):(3 - 5). As an implementation manner, the mass ratio of the activated waste FCC catalyst to attapulgite can specifically be 5:5, 6:4, or 7:3.

[0044] In the present invention, the volume ratio of the total mass of the activated waste FCC catalyst and attapulgite to water is preferably 1 g:(0.8 - 0.9) mL. The present invention controls the volume ratio of the total mass of the activated waste FCC catalyst and attapulgite to water within the above ranges, which can make the mixing of each raw material more uniform.

[0045] In the present invention, the mixing of the activated waste FCC catalyst, attapulgite and water is preferably carried out under stirring conditions. The present invention has no special limitation on the manner and rate of the stirring, and the raw materials can be stirred evenly by adopting the stirring technical solutions well-known to those skilled in the art.

[0046] In the present invention, the drying temperature is preferably 100-120°C, more preferably 110°C; the drying time is preferably 8-10 h.

[0047] After drying is completed, the present invention preferably crushes the dried product and then sieves it.

[0048] In the present invention, the particle size of the SFCC-PG support is preferably 30-60 mesh.

[0049] The present invention has no special limitation on the operations of crushing and sieving, and the technical solutions of crushing and sieving well-known to those skilled in the art can be adopted to ensure that the particle size of the SFCC-PG support is within the above range.

[0050] After obtaining the SFCC-PG support, the present invention impregnates the SFCC-PG support in an equal volume in a vanadium source solution, stirs it evenly, and then performs static settling, freezing and heating drying in sequence to obtain vanadium source / SFCC-PG.

[0051] In the present invention, the vanadium source solution is preferably an oxalic acid solution of ammonium metavanadate.

[0052] In the present invention, the concentration of ammonium metavanadate in the vanadium source solution is preferably 0.051-0.085 g / mL.

[0053] In the present invention, the concentration of oxalic acid in the vanadium source solution is preferably 0.08-0.13 g / mL.

[0054] In the present invention, the impregnation is preferably carried out under stirring conditions. The present invention has no special limitation on the manner and rate of the stirring, and the SFCC-PG support and the vanadium source solution can be stirred evenly by adopting the stirring technical solutions well-known to those skilled in the art.

[0055] In the present invention, the temperature for static settling is preferably room temperature; the time for static settling is preferably 4-6 h, more preferably 5 h.

[0056] In the present invention, the temperature for freezing is preferably -45 to -40°C, more preferably -45°C; the time for freezing is preferably 1-2 h, more preferably 2 h.

[0057] In the present invention, the heating drying is preferably as follows: heating to 20-30°C at a heating rate of 1-3°C / h.

[0058] After obtaining the vanadium source / SFCC-PG, the cerium salt solution is dropped onto the surface of the vanadium source / SFCC-PG in the present invention, and then static standing, freezing, heating and drying, and calcination are carried out in sequence to obtain V 2 O 5 -CeO 2 / SFCC-PG catalytic / adsorbent.

[0059] In the present invention, the cerium salt solution is preferably an aqueous solution of a cerium salt.

[0060] In the present invention, the cerium salt in the cerium salt solution is preferably cerium nitrate or cerium acetate.

[0061] In the present invention, the concentration of the cerium salt solution is preferably 0.065 to 0.26 g / mL. As an implementation manner, the concentration of the cerium salt solution can specifically be 0.065 g / mL, 0.13 g / mL, or 0.26 g / mL.

[0062] In the present invention, the mass ratio of the vanadium source / SFCC-PG to the volume of the cerium salt solution is preferably 1 g:(0.7 to 0.9) mL, more preferably 1 g:0.8 mL.

[0063] The present invention has no special limitation on the dropping operation, and the dropping technical solution well-known to those skilled in the art can be adopted to ensure that the cerium salt solution is uniformly dropped onto the surface of the vanadium source / SFCC-PG.

[0064] In the present invention, the temperature for static standing is preferably room temperature; the time for static standing is preferably 4 to 6 h, more preferably 5 h.

[0065] In the present invention, the temperature for freezing is preferably -45 to -40 °C, more preferably -45 °C; the time for freezing is preferably 1 to 2 h, more preferably 2 h.

[0066] In the present invention, the heating and drying is preferably: heating to 20 to 30 °C at a heating rate of 1 to 3 °C / h.

[0067] In the present invention, the temperature for calcination is preferably 450 to 550 °C. As an implementation manner, the temperature for calcination can specifically be 450 °C, 460 °C, 470 °C, 480 °C, 490 °C, 500 °C, 510 °C, 520 °C, 530 °C, 540 °C, or 550 °C.

[0068] In the present invention, the time for calcination is preferably 2 to 4 h. As an implementation manner, the time for calcination can specifically be 2 h, 2.5 h, 3 h, 3.5 h, or 4 h.

[0069] In the present invention, the calcination is preferably carried out in an oxygen or air atmosphere. In the present invention, during the calcination process, the cerium salt forms CeO 2 , and the vanadium source generates V 2 O 5 . By controlling the calcination temperature and time within the above ranges in the present invention, the cerium salt can fully react to form CeO 2 , and the vanadium source can fully react to form V 2 O 5 .

[0070] The preparation method of the present invention is simple and easy to implement.

[0071] The present invention also provides the use of the V 2 O 5 -CeO 2 / SFCC-PG catalyst / adsorbent described in the above technical solution or the V 2 O 5 -CeO 2 / SFCC-PG catalyst / adsorbent prepared by the preparation method described in the above technical solution for removing Hg 0 from flue gas.

[0072] In the present invention, the V 2 O 5 -CeO 2 / SFCC-PG catalyst / adsorbent is preferably loaded into a fixed-bed reactor, and flue gas containing Hg 0 is introduced to carry out catalytic-adsorption to obtain purified flue gas.

[0073] In the present invention, the concentration of Hg 0 in the flue gas containing Hg 0 is preferably 20-200 μg / m 3 ; the space velocity of the flue gas containing Hg 0 is preferably 5000-20000 h -1 .

[0074] In the present invention, the temperature of the catalytic-adsorption is preferably 150-250 °C.

[0075] The catalyst / adsorbent of the present invention has high catalytic oxidation activity and adsorption capacity for Hg 0 within the range of exhaust gas, and can catalytically oxidize Hg 0 in the flue gas to form Hg 2+ compounds. At the same time, the generated Hg 2+ compounds are adsorbed in the catalyst / adsorbent, and no post-treatment is required. It can be placed at the end of the flue gas purification system of a coal-fired power plant without reheating the flue gas again; sulfur dioxide in the flue gas not only has no poisoning effect on the catalyst / adsorbent, but instead promotes its removal of Hg 0It has a certain promoting effect. The catalyst / adsorbent of the present invention can be regenerated and recycled, and at the same time, the problem of secondary pollution is solved, having good application prospects.

[0076] Next, the technical solutions in the present invention will be clearly and completely described in conjunction with the embodiments in the present invention. Obviously, the described embodiments are only a part of the embodiments of the present invention, rather than all of the embodiments. Based on the embodiments in the present invention, all other embodiments obtained by those of ordinary skill in the art without making creative efforts fall within the protection scope of the present invention.

[0077] Example 1

[0078] A V 2 O 5 -CeO 2 / SFCC-PG catalyst / adsorbent, which consists of an SFCC-PG support and V 2 O 5 and CeO 2 loaded on the surface of the SFCC-PG support; the mass ratio of SFCC to PG in the SFCC-PG support is 6:4, and the total mass of V 2 O 5 and CeO 2 is 6% of the total mass of the catalyst / adsorbent, and the mass ratio of V 2 O 5 and CeO 2 is 5:1;

[0079] The preparation method of the V 2 O 5 -CeO 2 / SFCC-PG catalyst / adsorbent is as follows: (1) Roast the waste FCC catalyst in a muffle furnace at 500 °C in an air atmosphere for 1 h, and cool to obtain the activated waste FCC catalyst;

[0080] (2) Mix the activated waste FCC catalyst and attapulgite according to a mass ratio of 6:4, add water (the volume ratio of the total mass of the activated waste FCC catalyst and attapulgite to water is 1 g: 0.8 mL), stir evenly, dry at 110 °C for 10 h, crush, and sieve to obtain an SFCC-PG support with a particle size of 30-60 mesh;

[0081] (3) Equally impregnate 10 g of the SFCC-PG support obtained in step (2) with 8 mL of ammonium metavanadate (NH 4 VO 3in the oxalic acid solution (the concentration of ammonium metavanadate is 0.085 g / mL and the concentration of oxalic acid is 0.13 g / mL), stir evenly, let it stand at room temperature for 5 h, freeze at -45 °C for 2 h, and then heat it to 25 °C at a heating rate of 2 °C / h to obtain the vanadium source / SFCC-PG;

[0082] (4) Drop 8 mL of 0.13 g / mL cerium nitrate solution onto the surface of 10 g of the vanadium source / SFCC-PG obtained in step (3), let it stand at room temperature for 5 h, freeze at -45 °C for 2 h, then heat it to 25 °C at a heating rate of 2 °C / h, and finally calcine it at 500 °C for 3 h in an air atmosphere to obtain 5% V 2 O 5 -1% CeO 2 / SFCC-PG catalytic / adsorbent.

[0083] Load the 5% V 2 O 5 -1% CeO 2 / SFCC-PG catalytic / adsorbent obtained in Example 1 into a fixed-bed quartz tube reactor, and introduce simulated flue gas containing Hg 0 (N 2 + 5% O 2 + 0.15% SO 2 + 0.05% NO + 5% H 2 O + 200 μg·m -3 Hg 0 ), and carry out a constant-temperature adsorption reaction for 5 h at 150 °C and an airspeed of 5000 h -1 The removal efficiency of Hg 0 is 97%.

[0084] Load the 5% V 2 O 5 -1% CeO 2 / SFCC-PG catalytic / adsorbent obtained in Example 1 into a fixed-bed quartz tube reactor, and introduce simulated flue gas containing Hg 0 (N 2 + 5% O 2 + 0.15% SO 2 + 0.06% NO + 5% H 2 O + 80 μg·m -3 Hg 0 ), and carry out a constant-temperature adsorption reaction for 5 h at 250 °C and an airspeed of 5000 h -1 The removal efficiency of Hg 0 is 87%.

[0085] Load the 5% V 2 O 5 -1% CeO 2The / SFCC-PG catalyst / adsorbent was loaded into a fixed-bed quartz tube reactor, and simulated flue gas containing Hg 0 was introduced (N 2 + 5% O 2 + 0.15% SO 2 + 0.05% NO + 5% H 2 O + 80 μg·m -3 Hg 0 ). Under the conditions of 150 °C and a space velocity of 15000 h -1 , the constant-temperature adsorption reaction was carried out for 5 h, and the removal efficiency of Hg 0 was 93%.

[0086] The 5% V 2 O 5 -1% CeO 2 / SFCC-PG catalyst / adsorbent in Example 1 was loaded into a fixed-bed quartz tube reactor, and simulated flue gas containing Hg 0 was introduced (N 2 + 5% O 2 + 0.15% SO 2 + 0.06% NO + 5% H 2 O + 200 μg·m -3 Hg 0 ). Under the conditions of 200 °C and a space velocity of 10000 h -1 , the constant-temperature adsorption reaction was carried out for 5 h, and the removal efficiency of Hg 0 was 90%.

[0087] The 5% V 2 O 5 -1% CeO 2 / SFCC-PG catalyst / adsorbent in Example 1 was loaded into a fixed-bed quartz tube reactor, and simulated flue gas containing Hg 0 was introduced (N 2 + 5% O 2 + 0.15% SO 2 + 0.05% NO + 5% H 2 O + 80 μg·m -3 Hg 0 ). Under the conditions of 150 °C and a space velocity of 20000 h -1 , the constant-temperature adsorption reaction was carried out for 5 h, and the removal efficiency of Hg 0 was 85%.

[0088] Example 2

[0089] A V 2 O 5 -CeO 2 / SFCC-PG catalyst / adsorbent, consisting of an SFCC-PG support and V 2 O 5 and CeO 2 supported on the surface of the SFCC-PG support; the mass ratio of SFCC to PG in the SFCC-PG support is 5:5, and the total mass of V 2 O 5 and CeO 2 is 5% of the total mass of the catalyst / adsorbent, and the mass ratio of V 2 O 5 and CeO 2 is 3:2;

[0090] The preparation method of the V 2 O 5 -CeO 2 / SFCC-PG catalyst / adsorbent is as follows: (1)-(2) are the same as in Example 1 to obtain an SFCC-PG support with a particle size of 30-60 mesh;

[0091] (3) Immerse 10 g of the SFCC-PG support obtained in step (2) in 8 mL of an oxalic acid solution of ammonium metavanadate (NH 4 VO 3 ) (the concentration of ammonium metavanadate is 0.051 g / mL and the concentration of oxalic acid is 0.08 g / mL), stir evenly, let it stand at room temperature for 5 h, freeze at -40 °C for 2 h, and then heat it to 25 °C at a heating rate of 2 °C / h to obtain vanadium source / SFCC-PG;

[0092] (4) Drop 8 mL of a cerium nitrate solution with a concentration of 0.26 g / mL onto the surface of 10 g of the vanadium source / SFCC-PG obtained in step (3), let it stand at room temperature for 5 h, freeze at -40 °C for 1 h, then heat it to 25 °C at a heating rate of 2 °C / h, and finally calcine it in an air atmosphere at 500 °C for 3 h to obtain 3% V 2 O 5 -2% CeO 2 / SFCC-PG catalyst / adsorbent.

[0093] Load the 3% V 2 O 5 -2% CeO 2 / SFCC-PG catalyst / adsorbent in Example 2 into a fixed-bed quartz tube reactor, and introduce simulated flue gas containing Hg 0 (N 2 + 5% O 2 + 0.15% SO 2 + 0.05% NO + 5% H 2 O + 20 μg·m -3 Hg 0), at 150 °C and a space velocity of 5000 h -1 The constant-temperature adsorption reaction was carried out for 5 h under the conditions, and the removal efficiency of Hg 0 was 95%.

[0094] Example 3

[0095] A V 2 O 5 -CeO 2 / SFCC-PG catalyst / adsorbent, which consists of an SFCC-PG support and V 2 O 5 and CeO 2 loaded on the surface of the SFCC-PG support; the mass ratio of SFCC to PG in the SFCC-PG support is 7:3, and the total mass of V 2 O 5 and CeO 2 is 5.5% of the total mass of the catalyst / adsorbent, and the mass ratio of V 2 O 5 and CeO 2 is 5:0.5;

[0096] The preparation method of the V 2 O 5 -CeO 2 / SFCC-PG catalyst / adsorbent is as follows: (1)-(2) are the same as in Example 1 to obtain an SFCC-PG support with a particle size of 30-60 mesh;

[0097] (3) Immerse 10 g of the SFCC-PG support obtained in step (2) in 8 mL of an oxalic acid solution of ammonium metavanadate (NH 4 VO 3 )(the concentration of ammonium metavanadate is 0.085 g / mL and the concentration of oxalic acid is 0.08 g / mL), stir evenly, stand at room temperature for 5 h, freeze at -45 °C for 2 h, and then heat up to 25 °C at a heating rate of 2 °C / h to obtain a vanadium source / SFCC-PG;

[0098] (4) Drop 8 mL of a cerium nitrate solution with a concentration of 0.065 g / mL onto the surface of 10 g of the vanadium source / SFCC-PG obtained in step (3), stand at room temperature for 5 h, freeze at -45 °C for 2 h, then heat up to 25 °C at a heating rate of 2 °C / h, and finally calcine in an air atmosphere at 500 °C for 3 h to obtain a 5% V 2 O 5 -0.5% CeO 2 / SFCC-PG catalyst / adsorbent.

[0099] The 5% V 2 O 5 -0.5% CeO in Example 32 The / SFCC-PG catalyst / adsorbent was loaded into a fixed-bed quartz tube reactor, and simulated flue gas containing Hg 0 (N 2 + 5% O 2 + 0.15% SO 2 + 0.05% NO + 5% H 2 O + 20 μg·m -3 Hg 0 ) was introduced. The constant-temperature adsorption reaction was carried out for 5 h at 150 °C and a space velocity of 5000 h -1 . The removal efficiency of Hg 0 was 95%.

[0100] In summary, the catalyst / adsorbent provided by the present invention has excellent catalytic and adsorption properties for Hg 0 at a relatively low temperature.

[0101] The above are only the preferred embodiments of the present invention. It should be noted that for those of ordinary skill in the art, without departing from the principle of the present invention, several improvements and modifications can be made, and these improvements and modifications should also be regarded as the protection scope of the present invention.

Claims

1. A V2O5-CeO2 / SFCC-PG catalyst / adsorbent, comprising a SFCC-PG carrier and V2O5 and CeO2 loaded on the surface of the SFCC-PG carrier.

2. The V2O5-CeO2 / SFCC-PG catalyst / adsorbent according to claim 1, characterized in that: The mass ratio of SFCC to PG in the SFCC-PG carrier is (5-7): (3-5).

3. The V2O5-CeO2 / SFCC-PG catalyst / adsorbent according to claim 1, characterized in that: The total mass of the V2O5 and CeO2 is 1-10% of the total mass of the V2O5-CeO2 / SFCC-PG catalyst / adsorbent.

4. The V2O5-CeO2 / SFCC-PG catalyst / adsorbent according to claim 1, characterized in that: The mass ratio of V2O5 to CeO2 is (3-5):(0.5-2).

5. The method for preparing the V2O5-CeO2 / SFCC-PG catalyst / adsorbent according to any one of claims 1 to 4, comprising the following steps: (1) calcining the spent FCC catalyst to obtain an activated spent FCC catalyst; (2) mixing the activated spent FCC catalyst obtained in step (1) with attapulgite and water, and drying and sieving in sequence to obtain a SFCC-PG carrier; (3) immersing an equal volume of the SFCC-PG carrier obtained in step (2) in a vanadium source solution, and then sequentially placing the carrier at rest, freezing the carrier, and drying the carrier at elevated temperatures to obtain a vanadium source / SFCC-PG; (4) adding a cerium salt solution dropwise onto the surface of the vanadium source / SFCC-PG obtained in step (3), and then sequentially placing the mixture at rest, freezing, drying at elevated temperatures, and calcining the mixture to obtain a V2O5-CeO2 / SFCC-PG catalyst / adsorbent.

6. The preparation method according to claim 1, characterized in that: The calcination temperature in step (1) is 450-530° C., and the calcination time is 1-3 hours.

7. The preparation method according to claim 1, characterized in that: The particle size of the SFCC-PG carrier in step (2) is 30-60 meshes.

8. The preparation method according to claim 1, characterized in that: The vanadium source solution in step (3) is an oxalic acid solution of ammonium metavanadate.

9. The preparation method according to claim 1, characterized in that: The calcination temperature in step (4) is 450-550° C., and the calcination time is 2-4 hours.

10. The V2O5-CeO2 / SFCC-PG catalyst / adsorbent according to any one of claims 1 to 4 or the V2O5-CeO2 / SFCC-PG catalyst / adsorbent prepared by the preparation method according to any one of claims 5 to 9 is used for removing Hg from flue gas 0 application.