A method for desiliconizing oil
By adding organic compounds containing hydroxyl or carboxyl groups to the oil and contacting them with the silicon-collecting catalyst, the problem of removing complex silicon compounds from oil in existing technologies has been solved, achieving the removal of stable silicon compounds and protecting the activity of the refining catalyst.
Patent Information
- Authority / Receiving Office
- CN · China
- Patent Type
- Patents(China)
- Current Assignee / Owner
- CHINA PETROLEUM & CHEMICAL CORP
- Filing Date
- 2021-10-31
- Publication Date
- 2026-07-03
AI Technical Summary
Existing technologies are insufficient to effectively remove complex siloxanes and silane organosilicon compounds from oil products, leading to poisoning and deactivation of refining catalysts and affecting the refining process.
Adding organic compounds containing hydroxyl or carboxyl groups, such as alcohols or organic acids, to the feedstock oil allows them to come into contact with a silicon-scavenging catalyst, promoting the breakage and removal of stable silicon compounds.
Without altering the original reaction process, effective removal of difficult-to-remove silicon compounds was achieved, meeting the silicon content requirements of oil products and protecting the activity of refining catalysts.
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Abstract
Description
Technical Field
[0001] This invention belongs to the field of clean oil refining, and specifically relates to a method for desiliconizing oil products. Background Technology
[0002] Crude oil itself contains a large number of impurities, and some impurities are also introduced during the extraction process, such as silicon. Silicon can easily poison and deactivate refining catalysts. Therefore, silicon needs to be removed during crude oil refining. Silicon typically originates from defoamers in coking units; for example, the silicon content in coking gasoline is <10 ppm, and the silicon type is mainly cyclosiloxane-based silicon compounds. These silicon compounds are relatively easy to remove using existing technologies. However, organosilicon compounds such as siloxanes and silanes are difficult to remove due to their complex structures and high concentrations (hundreds or even thousands of ppm). These are very difficult to remove using existing technologies.
[0003] Existing technologies have many studies on oil desiliconization, which generally target traditional organosilicon compounds, usually considered to be cyclosiloxanes. Before hydrodesulfurization, treatment with general silicon-scavenging agents can meet the silicon content requirements of oil. For example, CN200710012085.5 discloses a method for hydrorefining silicon-containing distillate oil. The silicon-containing distillate oil feedstock and hydrogen are passed through at least two hydrorefining catalyst beds under hydrorefining conditions. The silicon-containing distillate oil feedstock first passes through a hydrorefining catalyst bed with silicon-scavenging function, and then passes through a conventional hydrorefining catalyst bed. The hydrorefining catalyst with silicon-scavenging function has a large pore volume and specific surface area and a relatively low metal content. CN201911020775.4 discloses an oil-based silica scavenger and its preparation method. The oil-based silica scavenger includes a carrier and a hydrogenation active component. The hydrogenation active component is a Group VIII metal sulfide, a Group VIB metal oxide, and a Group VIII metal oxide. Based on the total weight of the silica scavenger, the Group VIII metal sulfide is 0.1wt%-12.2wt%, the Group VIB metal oxide is 0.5wt%-17.2wt%, the Group VIII metal oxide is 0.1wt%-9.0wt%, and the carrier is 61.6%~90.3%. The preparation method includes the following: (1) impregnating the silica scavenger carrier with an impregnation solution containing a Group VIII metal, and then drying the material. The dried material is then subjected to sulfidation treatment; (2) impregnating the material after sulfidation in step (1) with an impregnation solution containing Group VIB and Group VIII metals, and then drying and calcining it under an inert atmosphere to obtain the oil-based silica scavenger. CN01138515.4 discloses a catalytic hydrotreating method for silica-containing naphtha. The method involves contacting a silica-containing hydrocarbon feedstock with a hydrotreating catalyst in the presence of hydrogen and under effective conditions for hydrotreating the feedstock. The improvement includes the step of adding 0.01-10 vol% water to the feedstock to wet the hydrotreating catalyst.
[0004] However, none of the above methods address the technical challenge of removing silicon effectively. Existing reaction systems cannot effectively remove these difficult-to-remove organosilicones such as siloxanes and silanes. New solutions are needed. Summary of the Invention
[0005] To address the aforementioned problems, this invention provides a method for desiliconizing oil products, which involves adding organic compounds containing hydroxyl or carboxyl groups to the raw oil to promote the removal of relatively stable silicon-containing compounds.
[0006] The present invention solves the above technical problems through the following technical solutions:
[0007] A method for desiliconizing oil includes the steps of mixing organic matter containing hydroxyl and / or carboxyl groups with the feed oil and contacting it with a silica-trapping catalyst.
[0008] Furthermore, the organic matter containing hydroxyl and / or carboxyl groups has a mass content of 0.01-5 wt% in the feedstock oil, preferably 0.5-3.5 wt%, and more preferably 1-2.5 wt%.
[0009] Furthermore, the organic compound containing hydroxyl and / or carboxyl groups is an alcohol or organic acid, more preferably a C1-C10 alcohol and / or acid, more preferably a C2-C8 alcohol and / or acid; and most preferably a C2-C6 alcohol and / or acid. The alcohol and / or acid includes monohydric alcohols, dihydric alcohols, trihydric alcohols, monobasic acids, dibasic acids, and tribasic acids. As a more specific embodiment, the organic compound containing hydroxyl and / or carboxyl groups is selected from at least one of ethanol, ethylene glycol, propanol, propylene glycol, glycerol, butanol, butanediol, glycerol, pentanol, acetic acid, oxalic acid, tartaric acid, succinic acid, glycolic acid, and citric acid.
[0010] Furthermore, the mixing of the organic matter containing hydroxyl and / or carboxyl groups with the feedstock oil is either pre-reactor mixing or simultaneous online mixing in the reactor. Pre-reactor mixing is preferred. As a more preferred technical solution, the organic matter containing hydroxyl and / or carboxyl groups is first mixed with the feedstock oil and preheated before being introduced into the reactor. The preheating temperature is 200-350°C, and the preheating time is 10 min-2 h, preferably 10 min-30 min.
[0011] Furthermore, the method of this invention is applicable to feedstock oils with a silicon content ranging from 1 to 3000 μg / g. Feedstock oils with high silicon content require several cycles of desilication treatment to reach the standard. Feedstock oils with a silicon content of 5-700 μg / g are preferred. The feedstock oil contains at least one silicon-containing compound other than cyclic siloxanes and silanes. The cyclic siloxanes are formed by cyclic siloxane bonds (-Si-O-). nOrganosilicon compounds with n≥3 as the main chain, such as those with the general formula (H2SiO). n Compounds with n≥3, or compounds in which H in the general formula is replaced by alkyl groups, halogens, etc.; the silane compounds are those having Si n H 2n+2 Organosilicon compounds of the general formula n≥1.
[0012] Furthermore, the silicon compounds in the feedstock include, but are not limited to, at least one of alkylsilanes, silanols, or silyl ethers containing silicon.
[0013] Furthermore, as a specific embodiment, the silicon compound in the feedstock oil includes, but is not limited to, at least one of tetramethylsilane, triethylsilane, tetraethylsilane, tetrapropylsilane, trimethylsilanol, dimethoxydimethylsilane, diethoxydimethylsilane, hexamethyldisiloxane, dimethyloctylchlorosilane, octamethyltrisiloxane, and n-octyltriethoxysilane.
[0014] The aforementioned silicon compounds are more stable than epoxy silane compounds or silane compounds. Existing desilication conditions and silicon-trapping catalysts are insufficient to remove them to meet requirements. This invention employs a method of adding organic compounds containing hydroxyl and / or carboxyl groups. The inventors have discovered that organic compounds containing hydroxyl and / or carboxyl groups facilitate the removal of the aforementioned stable silicon compounds. Specifically, the hydroxyl and carboxyl groups in the organic compounds may facilitate the breaking of Si-O or Si-C bonds, exposing Si atoms for removal by the silicon-trapping agent.
[0015] Furthermore, the feedstock may optionally contain epoxy silane compounds and / or silane compounds. These are a relatively common class of silicon-containing compounds in current feedstocks.
[0016] Furthermore, the process conditions for the contact reaction between the feedstock oil and the silica-collecting catalyst are: reaction pressure 1.0-10.0 MPa, hydrogen-to-oil volume ratio 80:1-800:1, and volume hourly space velocity 1-10.0 h⁻¹. -1 The reaction temperature is 150-450℃, preferably 250-350℃.
[0017] Furthermore, the silicon-trapping catalyst support is alumina, and the active metal is a Group VIB metal oxide and / or a Group VIII metal oxide. Based on the weight of the silicon-trapping catalyst, the content of the Group VIB metal oxide is 5%-30%, preferably 5%-15%, and the content of the Group VIII metal oxide is 1%-15%, preferably 2%-6%; the specific surface area is 100-500 m². 2 / g, preferably 300-500m 2 / g, pore volume is 0.3-1.2mL / g, preferably 0.4-0.8mL / g, and surface hydroxyl concentration is 300-2000μmol / g.
[0018] Furthermore, the preparation method of the silicon-capturing catalyst is well known in the art, and one or more of the following methods can be used: impregnation, co-extrusion, and co-precipitation.
[0019] Furthermore, the feedstock oil is one or more of the following: straight-run naphtha, hydrotreated naphtha, jet fuel, gasoline, diesel, wax oil, and residual oil.
[0020] This invention addresses a new problem in the desiliconization process of oil products in existing technologies, specifically the persistent issue of substandard desiliconization. First, the existing problem is clearly identified, primarily related to changes in the type of silicon-containing compounds in the oil. Through creative analysis and experimental research, a method is proposed to promote desiliconization by adding organic compounds containing hydroxyl or carboxyl groups to the oil. This method achieves unexpected technical results, enabling satisfactory silicon removal without altering the original reaction process conditions or silicon-capturing catalyst. This provides a practical and feasible technical solution for enterprises to address desiliconization problems.
[0021] Other features and advantages of the present invention will be described in detail in the following detailed description section. Detailed Implementation
[0022] The following non-limiting embodiments are intended to enable those skilled in the art to more fully understand the invention, but do not limit the invention in any way.
[0023] The catalyst composition provided by this invention can be characterized by a combination of inductively coupled plasma (ICP) and XRF spectroscopy, revealing the total content of Group VIB and Group VIII metals in the catalyst. The specific surface area and pore volume of the catalyst provided by this invention are analyzed using nitrogen physical adsorption, and the hydroxyl concentration on the catalyst surface is analyzed using infrared acid adsorption. The silicon content and type in the feedstock and product are analyzed using ICP and NMR, with ICP used to analyze the silicon content and 29Si MAS NMR used to analyze the silicon type. The silicon content and type deposited on the catalyst provided by this invention are analyzed using XRF and 29Si MAS NMR, with XRF used to analyze the silicon content deposited on the catalyst and 29Si MAS NMR used to analyze the silicon type deposited on the catalyst.
[0024] Silicon-trapping catalysts were prepared in Examples 1-3:
[0025] Example 1
[0026] An equal volume of solutions containing nickel salt and molybdenum salt was impregnated into an alumina support, then dried at 120°C for 3 hours in air, and calcined at 400°C for 3 hours to obtain silicon-collecting catalyst C-1.
[0027] The weight percentages of the components in the silicon-capturing catalyst C-1 are as follows: molybdenum oxide 20.1%, nickel oxide 4.5%, and the remainder is aluminum oxide. The catalyst properties are shown in Table 1.
[0028] Example 2
[0029] An equal volume of solutions containing nickel salt and molybdenum salt was impregnated into an alumina support, then dried at 110°C for 3 hours in air, and calcined at 350°C for 3 hours to obtain silicon-collecting catalyst C-2.
[0030] The weight percentages of the components in the silicon-trapping catalyst C-2 are as follows: molybdenum oxide 14.3%, nickel oxide 3.5%, and the remainder is aluminum oxide. The catalyst properties are shown in Table 1.
[0031] Example 3
[0032] An equal volume of solutions containing cobalt and molybdenum salts was impregnated into an alumina support, then dried at 110°C for 3 hours in air, and calcined at 450°C for 3 hours to obtain silicon-collecting catalyst C-3.
[0033] The weight percentages of the components in the silicon-trapping catalyst C-3 are as follows: molybdenum oxide 13.6%, cobalt oxide 5.5%, and the remainder is aluminum oxide. The catalyst properties are shown in Table 1.
[0034] Table 1.
[0035]
[0036] Example 4
[0037] The feedstock oil was naphtha supplied by a Sinopec refinery. The silicon content in the feedstock oil was 353 μg / g. Nuclear magnetic resonance analysis showed that the silicon types were tetramethylsilane, triethylsilane, trimethylsilanol, and tetramethylcyclosiloxane.
[0038] The experiment was conducted using a 50 mL fixed-bed trickle hydrogenation apparatus. The catalyst was 10 g of C-1 catalyst, which was first subjected to sulfidation treatment under the following conditions: temperature 290 °C, hydrogen partial pressure 2.8 MPa, hydrogen-to-oil ratio 500:1, and volumetric hourly space velocity 2.0 h⁻¹. -1 Sulfurized oil is jet fuel with 3.0% CS2.
[0039] 1.0 wt% ethanol was added to naphtha, and then the mixture was pretreated in a heating tank at 250°C for 30 min. After catalyst sulfidation, the feed was switched to the preheated naphtha. The reaction conditions were: reaction temperature 300°C, hydrogen partial pressure 2.8 MPa, hydrogen-to-oil ratio 500:1, and volume hourly space velocity 6.0 h⁻¹. -1 After the reaction proceeded for 24 hours, the silicon content in the product was analyzed, as well as the silicon content and type deposited on the catalyst. The analytical results are shown in Table 2.
[0040] Comparative Example 1
[0041] The same naphtha feedstock as in Example 4 was used, except that no ethanol was added to the naphtha and it was fed directly. The catalyst, reactor and reaction conditions were the same as in Example 4.
[0042] The silicon content in the product was analyzed, as well as the silicon content and type deposited on the catalyst. The results are shown in Table 2.
[0043] Comparative Example 2
[0044] Except for the desilication reaction, which was conducted at a temperature of 340℃, all other procedures were the same as in Comparative Example 1. The silicon content in the product was analyzed, as were the silicon content and type deposited on the catalyst. The results are shown in Table 2.
[0045] Example 5
[0046] The feedstock oil was naphtha supplied by a Sinopec refinery. The silicon content of the feedstock oil was 647 μg / g. Nuclear magnetic resonance analysis showed that the silicon types were tetramethylsilane, dimethoxydimethylsilane, tetraethylsilane, and tetraethylcyclosiloxane.
[0047] The experiment was conducted using a 50 mL fixed-bed trickle hydrogenation apparatus. The catalyst was 10 g of C-2 catalyst, which underwent sulfidation treatment under the following conditions: temperature 290 °C, hydrogen partial pressure 2.8 MPa, hydrogen-to-oil ratio 500:1, and volumetric hourly space velocity 2.0 h⁻¹. -1 Sulfurized oil is jet fuel with 3.0% CS2.
[0048] Naphtha was pretreated by adding 1.0 wt% acetic acid and heating to 220°C for 30 min in a heating tank. After catalyst sulfidation, the feed was switched to the preheated naphtha. The reaction conditions were: reaction temperature 350°C, hydrogen partial pressure 2.8 MPa, hydrogen-to-oil ratio 500:1, and volume hourly space velocity 8.0 h⁻¹. -1 After the reaction proceeded for 24 hours, the silicon content in the product was analyzed, as well as the silicon content and type deposited on the catalyst. The analytical results are shown in Table 2.
[0049] Example 6
[0050] After adding 1.0 wt% acetic acid to naphtha, it was not preheated and directly entered the hydrogenation unit, otherwise the same as in Example 5.
[0051] Comparative Example 3
[0052] The same naphtha feedstock as in Example 5 was used, except that acetic acid was not added to the naphtha and it was fed directly. The catalyst, reactor and reaction conditions were the same as in Example 5.
[0053] The silicon content in the product was analyzed, as well as the silicon content and type deposited on the catalyst. The results are shown in Table 2.
[0054] Example 7
[0055] The evaluation feedstock was naphtha supplied by a Sinopec refinery. The silicon content of the feedstock was 908 μg / g. Nuclear magnetic resonance analysis showed that the silicon types were diethoxydimethylsilane, hexamethyldisiloxane, and tetrapropylsilane.
[0056] The experiment was conducted using a 50 mL fixed-bed trickle hydrogenation apparatus. The catalyst was 10 g of C-3 catalyst, which underwent sulfidation treatment under the following conditions: temperature 290 °C, hydrogen partial pressure 2.8 MPa, hydrogen-to-oil ratio 500:1, and volumetric hourly space velocity 2.0 h⁻¹. -1 Sulfurized oil is jet fuel with 3.0% CS2.
[0057] Naphtha was pretreated by adding 1.5 wt% succinic acid to it and heating it to 220°C for 30 min in a heating tank. After sulfidation, the feed was switched to the preheated naphtha described above. The process conditions were: reaction temperature 320°C, hydrogen partial pressure 2.8 MPa, hydrogen-to-oil ratio 500:1, and volumetric hourly space velocity 4.0 h⁻¹. -1 After the reaction proceeded for 24 hours, the silicon content in the product was analyzed, as well as the silicon content and type deposited on the catalyst. The analytical results are shown in Table 2.
[0058] Comparative Example 4
[0059] The same naphtha feedstock as in Example 7 was used, except that succinic acid was not added to the naphtha and it was fed directly. The catalyst, reactor and reaction conditions were the same as in Example 7.
[0060] The silicon content in the product was analyzed, as well as the silicon content and type deposited on the catalyst. The results are shown in Table 2.
[0061] Example 8
[0062] The evaluation feedstock was naphtha supplied by a Sinopec refinery. The silicon content of the feedstock was 1208 μg / g. Nuclear magnetic resonance analysis showed that the silicon types were tetraethylsilane, tetramethylsilane, tetramethylcyclosiloxane, and n-octyltriethoxysilane.
[0063] The experiment was conducted using a 50 mL fixed-bed trickle hydrogenation apparatus. The catalyst was 10 g of C-3 catalyst, which underwent sulfidation treatment under the following conditions: temperature 290 °C, hydrogen partial pressure 2.8 MPa, hydrogen-to-oil ratio 500:1, and volumetric hourly space velocity 2.0 h⁻¹. -1 Sulfurized oil is jet fuel with 3.0% CS2.
[0064] 1.5 wt% ethylene glycol was added to naphtha and pretreated in a heating tank at 220°C for 30 min. After sulfidation, the feed was switched to the preheated naphtha described above. The process conditions were: reaction temperature 350°C, hydrogen partial pressure 2.8 MPa, hydrogen-to-oil ratio 500:1, and volumetric hourly space velocity 6.0 h⁻¹. -1 After the reaction proceeded for 24 hours, the silicon content in the product was analyzed, as well as the silicon content and type deposited on the catalyst. The analytical results are shown in Table 2.
[0065] Comparative Example 5
[0066] The same naphtha feedstock as in Example 8 was used, except that ethylene glycol was not added to the naphtha and it was fed directly. The catalyst, reactor and reaction conditions were the same as in Example 8.
[0067] The silicon content in the product was analyzed, as well as the silicon content and type deposited on the catalyst. The results are shown in Table 2.
[0068] Example 9
[0069] The evaluation feedstock was naphtha supplied by a Sinopec refinery. The silicon content of the feedstock was 632 μg / g. Nuclear magnetic resonance analysis showed that the silicon types were tetraethylsilane, tetramethylsilane, tetramethylcyclosiloxane, and n-octyltriethoxysilane.
[0070] The experiment was conducted using a 50 mL fixed-bed trickle hydrogenation apparatus. The catalyst was 10 g of C-3 catalyst, which underwent sulfidation treatment under the following conditions: temperature 290 °C, hydrogen partial pressure 2.8 MPa, hydrogen-to-oil ratio 500:1, and volumetric hourly space velocity 2.0 h⁻¹. -1 Sulfurized oil is jet fuel with 3.0% CS2.
[0071] Add 1.5 wt% ethylene glycol to naphtha. After sulfidation, switch to the above-mentioned naphtha feedstock. The process conditions are: reaction temperature 340℃, hydrogen partial pressure 2.8 MPa, hydrogen-to-oil ratio 500:1, and volumetric hourly space velocity 5.0 h⁻¹. -1 After the reaction proceeded for 24 hours, the silicon content in the product and the silicon content deposited on the catalyst were analyzed. The results are shown in Table 2.
[0072] Example 10
[0073] Except that the ethylene glycol content added to the naphtha is changed to 0.5 wt%, everything else is the same as in Example 9.
[0074] Example 11
[0075] Except that the ethylene glycol content added to the naphtha is changed to 0.5 wt%, everything else is the same as in Example 9.
[0076] Comparative Example 6
[0077] The same naphtha feedstock as in Example 9 was used, except that ethylene glycol was not added to the naphtha and it was fed directly. The catalyst, reactor and reaction conditions were the same as in Example 9.
[0078] The silicon content in the product and the silicon content deposited on the catalyst were analyzed. The results are shown in Table 2.
[0079] Example 12
[0080] The feedstock, reaction equipment, catalyst, and sulfidation process used are the same as in Example 9.
[0081] Add 2.0 wt% hexanol to naphtha. After sulfidation, switch to the above-mentioned naphtha feedstock. The process conditions are: reaction temperature 340℃, hydrogen partial pressure 2.8 MPa, hydrogen-to-oil ratio 600:1, and volumetric hourly space velocity 4.0 h⁻¹. -1 After the reaction proceeded for 24 hours, the silicon content in the product and the silicon content deposited on the catalyst were analyzed. The analytical results are shown in Table 2.
[0082] Comparative Example 7
[0083] The same naphtha feedstock as in Example 12 was used, except that hexanol was not added to the naphtha and it was fed directly. The catalyst, reactor and reaction conditions were the same as in Example 12.
[0084] The silicon content in the product and the silicon content deposited on the catalyst were analyzed. The results are shown in Table 2.
[0085] Example 13
[0086] The feedstock, reaction equipment, catalyst, and sulfidation process used are the same as in Example 9.
[0087] Add 1.5 wt% heptanoic acid to naphtha. After sulfidation, switch to the above-mentioned naphtha feedstock. The process conditions are: reaction temperature 350℃, hydrogen partial pressure 2.8 MPa, hydrogen-to-oil ratio 500:1, and volume hourly space velocity 5.0 h⁻¹. -1 After the reaction proceeded for 24 hours, the silicon content in the product and the silicon content deposited on the catalyst were analyzed. The results are shown in Table 2.
[0088] Comparative Example 8
[0089] The same naphtha feedstock as in Example 13 was used, except that no heptanoic acid was added to the naphtha and it was fed directly. The catalyst, reactor and reaction conditions were the same as in Example 13.
[0090] The silicon content in the product and the silicon content deposited on the catalyst were analyzed. The results are shown in Table 2.
[0091] Table 2.
[0092]
[0093] The silicon types deposited on the catalysts in the examples and comparative examples are mainly Si(OSi)3(OX), Si(OSi)2(OX)2, Si(OSi)(OX)3, Si(OX)4, Si(OSi)3(OX), and Si(OSi)2(OX)2 (X can be H, Al, or Si).
[0094] The evaluation results in Table 2 demonstrate that the oil desiliconization method of the present invention can effectively remove silicon from raw oil that is difficult to remove using conventional methods.
Claims
1. A method for desiliconizing an oil product, comprising the steps of mixing an organic compound containing hydroxyl and / or carboxyl groups with a feedstock oil and contacting it with a silica-collecting catalyst; wherein the organic compound containing hydroxyl and / or carboxyl groups has a mass content of 0.01-5 wt% in the feedstock oil; wherein the organic compound containing hydroxyl and / or carboxyl groups is selected from at least one of ethanol, ethylene glycol, propanol, propylene glycol, glycerol, butanol, butanediol, glycerol, pentanol, acetic acid, oxalic acid, tartaric acid, succinic acid, glycolic acid, and citric acid; and wherein the feedstock oil contains at least one silicon-containing compound selected from alkylsilanes, silanols, or silyl ethers.
2. The desilication method according to claim 1, characterized in that, The organic matter containing hydroxyl and / or carboxyl groups has a mass content of 0.5-3.5 wt% in the feed oil.
3. The desilication method according to claim 2, characterized in that, The organic matter containing hydroxyl and / or carboxyl groups has a mass content of 1-2.5 wt% in the feed oil.
4. The desilication method according to claim 1, characterized in that, The organic matter containing hydroxyl and / or carboxyl groups is mixed with the feedstock oil either before the reactor or by simultaneously introducing both into the reactor for online mixing.
5. The desilication method according to claim 4, characterized in that, The organic compounds containing hydroxyl and / or carboxyl groups are first mixed with the feed oil and preheated before being introduced into the reactor. The preheating temperature is 200-350℃ and the preheating time is 10min-2h.
6. The desilication method according to claim 1, characterized in that, The suitable feedstock oil has a silicon content of 1-3000 μg / g.
7. The desilication method according to claim 6, characterized in that, The silicon content in the feedstock oil suitable for processing is 5-700 μg / g.
8. The desilication method according to claim 1, characterized in that, The silicon-containing compound in the feedstock is selected from at least one of tetramethylsilane, triethylsilane, tetraethylsilane, tetrapropylsilane, trimethylsilanol, dimethoxydimethylsilane, diethoxydimethylsilane, hexamethyldisiloxane, dimethyloctylchlorosilane, octamethyltrisiloxane, and n-octyltriethoxysilane.
9. The desilication method according to claim 1, characterized in that, The process conditions for the reaction of the raw oil with the silicon-trapping catalyst are: reaction pressure 1.0-10.0 MPa, hydrogen / oil volume ratio 80:1-800:1, volume space velocity 1-10.0 h -1 -1, and reaction temperature 150-450°C.
10. The desilication method according to claim 9, characterized in that, The reaction temperature for the contact reaction between the feedstock oil and the silica-collecting catalyst is 250-350℃.
11. The desilication method according to claim 1, characterized in that, The silicon-trapping catalyst support is alumina, and the active metal is a Group VIB metal oxide and / or a Group VIII metal oxide. Based on the weight of the silicon-trapping catalyst, the content of the Group VIB metal oxide is 5%-30%, and the content of the Group VIII metal oxide is 1%-15%; the specific surface area is 100-500 m². 2 / g, pore volume is 0.3-1.2mL / g, and surface hydroxyl concentration is 300-2000μmol / g.