A catalyst for the hydrodearbusation of olefin-containing hydrocarbon oil and a method for preparing the same

Abstract

The application discloses a hydrogenation catalyst for removing arsenic from an olefin-containing hydrocarbon oil product and a preparation method thereof. The preparation method comprises the following steps: preparing stable dispersion impregnation component A-1 by mixing organic complexing agent I, organic auxiliary agent II and deionized water; dissolving a component containing a group VIII metal in the stable dispersion impregnation component A-1 to form stable complex impregnation liquid A-2; impregnating a porous carrier Z with the stable complex impregnation liquid A-2, and then drying and calcining to obtain a catalyst C1; dissolving organic auxiliary agent III in deionized water, then impregnating the catalyst C1, and then drying and calcining to obtain a final hydrogenation catalyst C2. According to the preparation method, the arsenic capacity of the catalyst is improved, the loss of octane number is reduced, and the economic benefits of a refinery are improved under the premise that the single-metal-system catalyst has relatively high arsenic removal selectivity.

Description

Technical Field

[0001] This invention relates to a catalyst, particularly to a hydrodearsenic removal catalyst used in petroleum processing and its preparation method, and more specifically to a catalyst used in the hydrodearsenic removal process of gasoline containing olefin feedstocks and its preparation method. Background Technology

[0002] Hydrogenation technology is one of the main methods for improving the quality of oil products in my country. The refining industry routinely uses hydrogenation to reduce the content of impurities such as sulfur, nitrogen, and aromatics in oil products, thereby improving their quality. Arsenic compounds in the feedstock are poisons during the hydrogenation process. Even trace amounts of arsenic compounds can permanently poison and deactivate the catalyst, shortening the long-term operation of the unit and causing economic losses to the refinery. Therefore, arsenic compounds need to be removed beforehand to ensure the stable operation of subsequent units.

[0003] Common methods for removing arsenic from oil products include adsorption, oxidation, and hydrotreating. Hydrotreating offers high arsenic capacity, excellent removal efficiency, and long operating cycles, making it more suitable for production conditions with high arsenic content in feedstocks, low arsenic content in products, and long operating cycles. Hydrotreating differs from desulfurization; it involves permanent arsenic poisoning and is non-renewable. Unlike desulfurization, the principle of hydrotreating involves trace amounts of organic arsenic compounds readily combining with the d orbitals of Group VIII metals on the surface of conventional hydrotreating catalysts to form coordinate bonds (nickel, with its face-centered cubic structure, readily combines with arsenic to form hexagonal arsenides, hence nickel is commonly the primary active metal for arsenic removal). As temperature increases, a large number of arsenic atoms migrate into the catalyst interior, forming stable arsenide alloys, ultimately causing permanent deactivation of the poisoned sites. Therefore, hydrotreating permanently sacrifices a large number of arsenic poisoning sites. Currently, most gasoline arsenic removal catalysts used for olefin-containing feedstocks employ a single-nickel system. However, this system suffers from metal aggregation, forming nickel-aluminum spinel, which affects the distribution of arsenic poisoning sites on the catalyst surface and within the pores, resulting in a waste of active metal. Furthermore, due to unsuitable catalyst pore structures, insufficient space is provided for the diffusion of large arsenic compounds, and the arsenic poisoning sites within the catalyst pores are not fully utilized. Therefore, current single-nickel system hydroarsenic removal catalysts suffer from insufficient arsenic capacity.

[0004] Patent CN 1043151C discloses a single-nickel catalyst prepared on a macroporous alumina support with a dual-channel distribution. It requires reduction under H2 and N2 atmospheres during use and can reduce arsenic content to below 5 ppb. CN 102140C relates to an arsenic removal catalyst for hydrocarbons, with a single-nickel system as the active center and a macroporous alumina support. It requires at least 50% of the nickel-hydrogen gas to be reduced before use and can also reduce arsenic content to below 5 ppb. However, both of these existing technologies use reduction as a pretreatment method for the catalyst. Currently, most mainstream catalysts in conventional oil refining hydrotreating processes are in a sulfide state. Reduction activation increases start-up complexity. Furthermore, although this patent uses macroporous alumina, it does not consider the dispersion of active nickel within the pores, affecting the utilization rate of arsenic poisoning sites.

[0005] Patent CN 108246242B proposes a catalytic gasoline hydrodearsenic removal catalyst and its application. This technology uses hydrothermal treatment to modify the TiO2-Al2O3 composite support and uses a single nickel system to prepare the hydrodearsenic removal catalyst. The catalyst has good arsenic removal selectivity, and the arsenic removal selectivity can reach more than 99% when processing raw materials with an arsenic content of about 200 ppb. However, the catalyst involved in this invention only involves the improvement of the pores in the support preparation process, but does not address the issues of nickel metal dispersion and active metal diffusion within the pores. Therefore, the problems of low active metal utilization and insufficient active metal dispersion still exist.

[0006] Patent CN 108246302B proposes a catalyst for catalytic hydrogenation of gasoline and its application. This technology uses a hydrothermal modification of a bimetallic arsenic removal catalyst on a TiO2-Al2O3 composite support, which can reduce the arsenic content of the raw material from 200 ppb to below 20 ppb. Compared with the single nickel system, the bimetallic system has improved arsenic capacity and arsenic removal activity. However, since this invention uses a bimetallic system, its octane number loss will inevitably be higher than that of the single metal system. In addition, this invention does not address the dispersion problem within the metal channels after pore expansion.

[0007] Patent CN 106833731B proposes a catalyst for the hydrodearsenic removal of naphtha and its application method. The catalyst support is prepared by alternating titration with non-constant pH, resulting in a zinc oxide layered structure containing zinc aluminum spinel. The preparation process is complex and has high industrial production costs, making it difficult to achieve in actual production. At the same time, it does not address the issue of dispersing and utilizing active metals within the pores.

[0008] Patent CN 100388980C proposes a pseudoboehmite composition containing an organic pore-expanding agent. By adding an organic pore-expanding agent to the pseudoboehmite, macroporous alumina can be obtained after calcination. However, this invention does not address the dispersion and utilization of active metals within the pores.

[0009] Patent CN 102284295B proposes a method for preparing a hydrogenation catalyst impregnation solution and a method for preparing the catalyst. This invention uses water-soluble organic additives to reduce the surface tension of the impregnation solution, without calcination, and reduces the aggregation of metal particles, thereby effectively improving the hydrogenation activity of the hydrogenation catalyst for heavy aromatics. However, the catalyst preparation method involves deep desulfurization and denitrification, but does not address the arsenic removal selectivity in the gasoline hydrogenation arsenic removal process, nor does it address the utilization of metals within the pores.

[0010] Patent CN107812525A discloses a hydrogenation catalyst composition comprising hydrogenation catalyst I and hydrogenation catalyst II. The hydrogenation catalyst I, by volume and based on the hydrogenation catalyst composition, comprises 5-95%. Hydrogenation catalyst I comprises a support, a hydrogenation-active metal element, and a non-metallic auxiliary element, wherein the hydrogenation-active metal element contains Group VIB and Group VIII metal elements. The preparation method of hydrogenation catalyst I includes: subjecting a support loaded with a compound containing a hydrogenation-active metal element, a first organic complexing agent, and a non-metallic auxiliary element to a first drying and calcination to obtain a semi-finished catalyst; wherein, by dry basis and based on the dry weight of the semi-finished catalyst, the carbon content of the semi-finished catalyst is 0.01-0.5% by weight; loading a second organic complexing agent onto the semi-finished catalyst, and subjecting it to a second drying without calcination to obtain hydrogenation catalyst I. This technology is applied in the field of desulfurization and denitrification. The active metal and complex components are added together to the impregnation solution and then the carrier is impregnated. The poor dispersion of the active metal will cause the active metal to stack. In the field of hydrodearsenic removal, the stacking of active metal will cause the loss of arsenic poisoning sites. Therefore, the dispersion of the active metal needs to be further improved. In addition, the preparation method of the hydrogenation catalyst involved in this technology does not involve the utilization of metal in the pores.

[0011] Therefore, in order to solve the problems of active metal aggregation on the surface and in the channels of current single-metal system hydroarsenic removal catalysts, poor dispersion of arsenic poisoning sites, and insufficient arsenic capacity, it is necessary to provide a hydroarsenic removal catalyst for olefin-containing hydrocarbon oils and its preparation method. Summary of the Invention

[0012] To address the aforementioned technical problems, this invention provides a method for preparing a single-metal system arsenic removal catalyst via hydrotreating. The method involves impregnating the catalyst with a highly dispersed active metal impregnation solution during the pore-expanding process. This ensures that the active metal enters the pores for high-dispersion loading while the pores are expanded. Furthermore, a post-treatment process is used to further disperse the active metal on the catalyst surface and within the pores. By controlling the molecular weight of the activator, the secondary activation impregnation solution is ensured to enter the pores. This secondary dispersion of the active metal on the surface and within the pores helps reduce the formation of aluminum spinel and improves the dispersion of nickel on the surface and within the pores. This method ensures that the single-metal system catalyst maintains high arsenic removal selectivity while increasing the arsenic capacity of the catalyst, reducing octane number loss, and improving the economic efficiency of the refinery.

[0013] To achieve the above objectives, the present invention provides a method for preparing a hydrodearsenic removal catalyst for olefin-containing hydrocarbon oils, the method comprising the following steps:

[0014] (1) Organic complexing agent I, organic auxiliary agent II and deionized water are formulated into a stable dispersion impregnation component A-1;

[0015] (2) Dissolve the component containing Group VIII metal in the stable dispersion impregnation component A-1 to form a stable complex impregnation solution A-2;

[0016] (3) The porous support Z was impregnated with stable complex impregnation solution A-2, and then dried and calcined to obtain catalyst C1;

[0017] (4) Dissolve organic auxiliary agent III in deionized water, then impregnate catalyst C1, and after drying and calcination, obtain the final hydrogen arsenic removal catalyst C2.

[0018] Preferably, the porous carrier Z is one or more composite carriers selected from alumina, titanium dioxide, silicon dioxide, and magnesium oxide, and more preferably alumina.

[0019] Preferably, the component containing a Group VIII metal is a nickel salt, including at least one of nickel nitrate, nickel acetate, nickel sulfate, and nickel basic carbonate, more preferably nickel nitrate or nickel basic carbonate.

[0020] Preferably, the hydrodearsenic removal catalyst C2 contains 6-26 wt% NiO and 74-94 wt% support, more preferably 7-22 wt% NiO and 78-93 wt% support.

[0021] Preferably, the organic complexing agent I is ammonia or a hydroxy acid compound, wherein the hydroxy acid compound includes at least one of ethylene glycol, glyceric acid, malic acid, citric acid, tartaric acid, gluconic acid, acetic acid, oxalic acid, malonic acid, trichloroacetic acid, and monochloroacetic acid, and more preferably citric acid or ammonia.

[0022] Preferably, the organic additive II is an alcohol or a soluble organic pore expander, including one of glycerol, propylene glycol, 1,4-butanediol, pentaerythritol, ethylene glycol, polyethylene glycol, diethylene glycol, polyvinyl alcohol, sodium stearate, sodium carboxymethyl cellulose, and soluble starch, more preferably one of glycerol, ethylene glycol, polyethylene glycol, sodium carboxymethyl cellulose, and soluble starch.

[0023] Preferably, the amount of organic additive II added accounts for 1 to 21 wt% of the porous carrier Z, more preferably 2 to 16 wt%.

[0024] Preferably, in step (1), the temperature during the preparation of the stable dispersion impregnation component A-1 is 10-100°C, more preferably 20-100°C, the temperature does not exceed the boiling point of the organic auxiliary II, and the mixing time is 10-120 min.

[0025] Preferably, in step (2), the temperature during the preparation of the stable complex impregnation solution A-2 is 10-100°C, more preferably 20-100°C, the temperature does not exceed the boiling point of the organic auxiliary agent II, and the mixing time is 10-120 min.

[0026] Preferably, the organic additive III is an alcohol, including one of ethanol, glycerol, ethylene glycol, and polyethylene glycol.

[0027] Preferably, the molecular weight of the alcohol added to the organic auxiliary agent III is smaller than that of the organic auxiliary agent II.

[0028] Preferably, the amount of organic auxiliary agent III added is 1 to 14 wt% of catalyst C1, more preferably 2 to 9 wt%.

[0029] Preferably, in step (3) or step (4), after impregnation, it is necessary to let it stand for 1 to 7 hours before drying and roasting, more preferably 1 to 6 hours.

[0030] Preferably, in step (3) or step (4), the drying temperature is 50-150°C and the drying time is 3-6 hours, more preferably the drying temperature is 50-120°C; the calcination temperature is 300°C-600°C and the calcination time is 3-6 hours.

[0031] Preferably, in step (3) or step (4), the impregnation process is saturated impregnation or supersaturated impregnation, with saturated impregnation being preferred.

[0032] Preferably, the hydrodearsenic removal catalyst C2 is used in a sulfided form during the arsenic removal process in oil processing.

[0033] The present invention also provides a catalyst for the hydrodearsenic removal of olefin-containing hydrocarbon oils, which is obtained by the above preparation method.

[0034] Compared with the prior art, the present invention has at least the following advantages:

[0035] (1) In a single impregnation, a pre-dispersion impregnation method is adopted, in which the pore-expanding agent (i.e., organic agent II) and the dispersing and complexing agent (i.e., organic complexing agent I) are uniformly complexed and then complexed with the main active metal. This can make the active metal in a more dispersed complexing state, alleviate the problem of easy metal aggregation in the single metal system, improve the dispersion of the active metal and the number of arsenic poisoning sites, and thus improve the arsenic capacity.

[0036] (2) Organic additive II can be pre-dispersed and then complexed with active metal to form bonds. During the calcination process, it can uniformly load active metal while expanding the pores. This can not only improve the flowability of macromolecular arsenides in the pores, but also improve the dispersion and number of arsenic poisoning sites in the expanded pores, thereby improving the utilization rate of active sites in the pores.

[0037] (3) The active metal is dispersed and activated in a second time through post-treatment. The molecular weight of the activated molecule (i.e., organic auxiliary agent III) is controlled to be less than that of organic auxiliary agent II. This ensures that the secondary activation impregnation solution enters the pores and disperses the active metal on the surface and in the pores in a second time, thereby further improving the dispersion and effective utilization rate of arsenic poisoning sites on the surface and in the pores and increasing the arsenic capacity.

[0038] (4) Under the premise that the single-metal system catalyst has high arsenic removal selectivity, the arsenic capacity of the catalyst can be effectively improved, thereby improving the economic benefits of the refinery. Detailed Implementation

[0039] The technical solutions of the present invention are further described below through embodiments, but the technical solutions of the present invention are not limited to the following embodiments.

[0040] The catalyst supports used in the examples and comparative examples can be obtained by the following preparation methods. However, it should be noted that the following preparation methods are only intended to provide a feasible method for preparing the support and are not intended to limit the present invention. The supports and preparation methods of the present invention are not limited thereto:

[0041] 600g of boehmite was mixed with 12g of guar gum powder, and then a solution consisting of 26g of citric acid, 17mL of concentrated nitric acid, and 510g of water was added. D3.0 clover-shaped wet strips were prepared using a standard laboratory extruder, dried at 120℃, and then calcined at 850℃ for 6 hours to obtain carrier L1. The properties of carrier L1 are shown in Table 1.

[0042] Table 1 Physicochemical properties of the carrier

[0043] <![CDATA[Specific surface area, m 2 / g]]> 279 Pore ​​diameter, nm 13 Bulk density, g / 100L 65 Water absorption rate, mL / 100g 85

[0044] Example 1

[0045] 1g of sodium carboxymethyl cellulose and 3g of citric acid were dissolved in deionized water and mixed at 50°C for 60 min until a homogeneous and clear solution was obtained. Then, 55g of nickel nitrate was added, and the mixture was refluxed at 50°C for 120 min. The volume was adjusted to 43mL, and the mixture was mixed for 10 min until a homogeneous and clear solution was obtained. 50g of support L1 was weighed and impregnated with an equal volume for 6 hours. After drying at 120°C for 6 hours, the solution was calcined at 500°C for 6 hours to obtain catalyst C1-1. 4.5g of polyethylene glycol (100) was dissolved in deionized water and the solution was adjusted to a final volume. An equal volume of C1-1 was impregnated with this solution, dried at 100°C for 6 hours, and then calcined at 500°C for 6 hours to obtain hydroarsenic removal catalyst C2-1.

[0046] Example 2

[0047] 5g of polyethylene glycol (1000) and 1.5g of citric acid were dissolved in deionized water and mixed at 25°C for 30 min until a homogeneous and clear solution was obtained. Then, 43g of nickel nitrate was added and the volume was adjusted to 43mL. The mixture was mixed for 25 min until a homogeneous and clear solution was obtained. 50g of support L1 was weighed and impregnated with an equal volume. The mixture was allowed to stand for 6 hours, dried at 110°C for 6 hours, and then calcined at 550°C for 6 hours to obtain catalyst C1-2. 2.5g of polyethylene glycol (500) was dissolved in deionized water and the volume was adjusted. C1-2 was impregnated with an equal volume, dried at 110°C for 6 hours, and then calcined at 550°C for 6 hours to obtain hydroarsenic removal catalyst C2-2.

[0048] Example 3

[0049] 10.5 g of ethylene glycol and 1 g of citric acid were dissolved in deionized water and mixed at 25 °C for 40 min until a homogeneous and clear solution was obtained. Then, 68.4 g of nickel nitrate was added and the volume was adjusted to 43 mL. The mixture was stirred for 50 min until a homogeneous and clear solution was obtained. 50 g of support L1 was weighed and impregnated with an equal volume for 1 hour. After drying at 120 °C for 4 h, the solution was calcined at 600 °C for 3 h to obtain catalyst C1-3. 7 g of ethanol was dissolved in deionized water and the solution was adjusted to a constant volume. C1-3 was then impregnated with an equal volume, dried at 120 °C for 3 h, and calcined at 600 °C for 4 h to obtain hydroarsenic removal catalyst C2-3.

[0050] Example 4

[0051] 0.5 g of glycerol and 25 mL of 25% ammonia were mixed at 20 °C for 20 min until a homogeneous and clear solution was obtained. Then, 10.63 g of nickel acetate was added and the volume was adjusted to 43 mL. The mixture was then mixed for 20 min until a homogeneous and clear solution was obtained. 50 g of support L1 was weighed and impregnated with an equal volume. The mixture was allowed to stand for 6 hours, dried at 80 °C for 3 hours, and then calcined at 600 °C for 4 hours to obtain catalyst C1-4. 0.5 g of ethylene glycol was dissolved in deionized water and the volume was adjusted. 50 g of C1-4 was impregnated with an equal volume. The mixture was dried at 50 °C for 4 hours and then calcined at 300 °C for 3 hours to obtain the hydroarsenic removal catalyst C2-4.

[0052] Example 5

[0053] Dissolve 8g of soluble starch and 2g of citric acid in deionized water, mix at 50℃ for 50min until a homogeneous and clear solution is obtained, then add 15g of nickel nitrate to bring the volume to 43mL, mix for 20min until a homogeneous and clear solution is obtained, weigh 50g of support L1 and impregnate it with an equal volume for 5h, dry at 100℃ for 5h and calcine at 450℃ for 5h to obtain catalyst C1-5. Dissolve 1g of glycerol in deionized water to bring the volume to a constant, impregnate C1-5 with an equal volume, dry at 100℃ for 5h and calcine at 400℃ for 5h to obtain hydroarsenic removal catalyst C2-5.

[0054] Comparative Example 1

[0055] 0.5 g glycerol, 25 mL 25% ammonia water, and 10.63 g nickel acetate were mixed at 20 °C for 20 min until a homogeneous and clear solution was obtained. The solution was then brought to a final volume of 43 mL and mixed for another 20 min until a homogeneous and clear solution was obtained. 50 g of support L1 was weighed and impregnated with the solution in an equal volume. The solution was allowed to stand for 6 hours, dried at 80 °C for 3 hours, and then calcined at 600 °C for 4 hours to obtain catalyst D1.

[0056] Comparative Example 2

[0057] 10.63 g of nickel acetate and 25 mL of 25% ammonia water were mixed at 20 °C for 20 min until a homogeneous and clear solution was obtained. Then, 0.5 g of glycerol was added and the volume was adjusted to 43 mL. The mixture was mixed for 20 min until a homogeneous and clear solution was obtained. 50 g of support L1 was weighed and impregnated with an equal volume. After standing for 6 hours, the solution was dried at 80 °C for 3 h and then calcined at 600 °C for 4 h to obtain catalyst D2-1. 0.5 g of ethylene glycol was dissolved in deionized water and the volume was adjusted. 50 g of D2-1 was impregnated with an equal volume, dried at 50 °C for 4 h, and then calcined at 300 °C for 3 h to obtain the hydroarsenic removal catalyst D2.

[0058] Example 6

[0059] This embodiment relates to the catalyst evaluation of Examples 1 to 5 and Comparative Examples 1 to 2.

[0060] The catalyst evaluations for the above embodiments and comparative examples were conducted in a 30mL microreactor evaluation device using wet sulfidation. Carbon disulfide was used as the sulfiding agent at a dosage of 3wt%, and refined naphtha was used as the sulfiding oil. Hydrogen was passed through once. The sulfidation conditions were 230℃ and 320℃ for 8 hours each, with a sulfidation pressure of 2.0 MPa and a hydrogen-to-oil ratio of 300:1. After sulfidation, feedstock oil was introduced. A summary table of feedstock oil properties is shown in Table 2, and a summary table of reaction process parameters and products for each embodiment is shown in Table 3.

[0061] Arsenic content was analyzed using an Agilent ICP-MS 7850. Group composition analysis of the oil was performed using an Agilent PONA chromatographic analyzer.

[0062] The arsenic content test used the arsenic-containing raw materials listed in Table 2. The arsenic-containing raw materials were prepared by adding triethylarsenic (20 ppm) to the catalytic gasoline product oil and conducting the test at a temperature of 260℃, a pressure of 2 MPa, and a space velocity of 10 h⁻¹. -1 The arsenic removal reaction was carried out under the reaction conditions of hydrogen / oil = 300. When the arsenic removal rate of the product was <90%, the arsenic capacity experiment was stopped. The As2O3 content was determined by X-ray diffraction spectroscopy (XRF analysis) to obtain the arsenic capacity of the catalyst.

[0063] Table 2 Properties of Crude Oil

[0064]

[0065] Table 3 Summary of Evaluation Results

[0066]

[0067]

[0068] As shown in Table 3, the hydroarsenic removal catalyst prepared by the method of this invention, when treating olefin-containing gasoline feedstock, can meet the requirement of an arsenic content of less than 20 ppb while ensuring a low octane number loss. Furthermore, its arsenic capacity is higher than that of the catalyst prepared in the comparative example, exhibiting better long-term performance. Evaluation results indicate that during the arsenic removal process, the catalyst prepared by the method of this invention improves the dispersion of metallic nickel inside and outside the pores, thereby increasing the number of effective arsenic poisoning sites within the expanded pores. This improves the utilization rate of active sites within the pores, alleviating to some extent the problems of metal aggregation and low utilization rate of arsenic poisoning sites in single-metal systems, thus enhancing the arsenic removal activity and stability of the catalyst.

[0069] Of course, the present invention may have other embodiments and variations. Without departing from the spirit and essence of the present invention, those skilled in the art can make various corresponding changes and variations according to the present invention, but these corresponding changes and variations should all fall within the protection scope of the claims of the present invention.

Claims

1. A method for preparing a catalyst for the hydrodearsenic removal of olefin-containing hydrocarbon oils, characterized in that, Includes the following steps: (1) Complexing agent I, organic auxiliary agent II and deionized water are formulated into a stable dispersion impregnation component A-1; (2) Dissolve the component containing Group VIII metal in the stable dispersion impregnation component A-1 to form a stable complex impregnation solution A-2; (3) The porous support Z was impregnated with stable complex impregnation solution A-2, and then dried and calcined to obtain catalyst C1; (4) Dissolve organic auxiliary agent III in deionized water, then impregnate catalyst C1, and after drying and calcination, obtain the final hydrogen arsenic removal catalyst C2; The porous carrier Z is a composite carrier of one or more of the following: alumina, titanium dioxide, silicon dioxide, and magnesium oxide. The complexing agent I is ammonia or a hydroxy acid compound; The organic additive II is an alcohol or a soluble organic pore expander; The organic auxiliary agent III is an alcohol.

2. The preparation method according to claim 1, characterized in that, The porous carrier Z is alumina.

3. The preparation method according to claim 1, characterized in that, The component containing Group VIII metal is a nickel salt, including at least one of nickel nitrate, nickel acetate, nickel sulfate, and nickel basic carbonate.

4. The preparation method according to claim 1, characterized in that, The component containing Group VIII metal is a nickel nitrate or a nickel basic carbonate.

5. The preparation method according to claim 1, 3, or 4, characterized in that, The hydrogenated arsenic removal catalyst C2 contains 6-26 wt% NiO and 74-94 wt% support.

6. The preparation method according to claim 5, characterized in that, The hydrogenated arsenic removal catalyst C2 contains 7-22 wt% NiO and 78-93 wt% support.

7. The preparation method according to claim 1, characterized in that, The hydroxy acid compounds include at least one of ethylene glycol, glyceric acid, malic acid, citric acid, tartaric acid, gluconic acid, and lactic acid.

8. The preparation method according to claim 1, characterized in that, The complexing agent I is citric acid or ammonia.

9. The preparation method according to claim 1, characterized in that, The organic additive II includes one of the following: glycerol, propylene glycol, 1,4-butanediol, pentaerythritol, ethylene glycol, polyethylene glycol, diethylene glycol, polyvinyl alcohol, sodium stearate, sodium carboxymethyl cellulose, and soluble starch.

10. The preparation method according to claim 1, characterized in that, The organic additive II includes one of glycerol, ethylene glycol, polyethylene glycol, sodium carboxymethyl cellulose, and soluble starch.

11. The preparation method according to claim 1, characterized in that, The amount of organic additive II added accounts for 1 to 21 wt% of the porous carrier Z.

12. The preparation method according to claim 11, characterized in that, The amount of organic additive II added accounts for 2 to 16 wt% of the porous carrier Z.

13. The preparation method according to claim 1, characterized in that, In step (1) or step (2), the temperature during the preparation of the stable dispersed impregnation component A-1 or the stable complex impregnation solution A-2 is 10~100℃, the temperature does not exceed the boiling point of the organic auxiliary agent II, and the mixing time is 10min~120min.

14. The preparation method according to claim 1, characterized in that, The organic additive III includes one of ethanol, glycerol, ethylene glycol, and polyethylene glycol.

15. The preparation method according to claim 1, characterized in that, The molecular weight of the alcohol added to organic auxiliary agent III is smaller than that of organic auxiliary agent II.

16. The preparation method according to claim 1, characterized in that, The amount of organic auxiliary agent III added is 1 to 14 wt% of catalyst C1.

17. The preparation method according to claim 16, characterized in that, The amount of organic additive III added is 2 to 9 wt% of catalyst C1.

18. The preparation method according to claim 1, characterized in that, In step (3) or step (4), after impregnation, it is necessary to let it stand for 1 to 7 hours before drying and calcining; the drying temperature is 50 to 150°C and the drying time is 3 to 6 hours; the calcining temperature is 300°C to 600°C and the calcining time is 3 to 6 hours.

19. The preparation method according to claim 1, characterized in that, In step (3) or step (4), the impregnation process is saturated impregnation or supersaturated impregnation.

20. The preparation method according to claim 1, characterized in that, The hydro-dearsenic removal catalyst C2 is used in a sulfided form during the dearsenic removal process in oil processing.

21. A catalyst for the hydrodearsenic removal of olefin-containing hydrocarbon oils, characterized in that, It is obtained by the preparation method according to any one of claims 1-20.

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