CN111420670A - 一种加氢催化剂及其制备方法和应用 - Google Patents
一种加氢催化剂及其制备方法和应用 Download PDFInfo
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- VYPSYNLAJGMNEJ-UHFFFAOYSA-N silicon dioxide Inorganic materials O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims abstract description 13
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 claims abstract description 11
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- B—PERFORMING OPERATIONS; TRANSPORTING
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- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
- B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/84—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- B01J23/85—Chromium, molybdenum or tungsten
- B01J23/88—Molybdenum
- B01J23/883—Molybdenum and nickel
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
- B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/84—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- B01J23/85—Chromium, molybdenum or tungsten
- B01J23/88—Molybdenum
- B01J23/882—Molybdenum and cobalt
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J35/00—Catalysts, in general, characterised by their form or physical properties
- B01J35/30—Catalysts, in general, characterised by their form or physical properties characterised by their physical properties
- B01J35/396—Distribution of the active metal ingredient
- B01J35/399—Distribution of the active metal ingredient homogeneously throughout the support particle
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
- C10G45/04—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used
- C10G45/06—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof
- C10G45/08—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum, or tungsten metals, or compounds thereof
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
- C10G2300/202—Heteroatoms content, i.e. S, N, O, P
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
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- Y02P20/50—Improvements relating to the production of bulk chemicals
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Abstract
本发明公开了一种加氢催化剂及其制备方法和应用。所述加氢催化剂包括载体、钼和至少一种选自第VIII族的活性金属组分,所述载体是SiO2‑AlOOH复合物。本发明在铝盐的水解液中加入含硅源的水溶液,催化剂的表面酸性易于调节,B酸/L酸的摩尔比是0.5‑3.2;在载体SiO2‑AlOOH的合成过程中加入活性金属盐,使得最终形成的催化剂中活性金属在载体上均匀分散;合成的催化剂具有亲油性,容易在重油中均匀分散;与现有重油加氢处理催化剂相比,采用本发明的加氢催化剂能够获得更好的加氢脱硫、脱氮和裂化效果。
Description
技术领域
本发明涉及一种加氢催化剂及其制备方法和在重油悬浮床加氢中的应用,属于催化剂制备与应用技术领域。
背景技术
近年来全球市场上原油劣质化程度不断增加,而随着世界经济不断发展和各国环保法规愈加严格,如何高效加工重质原油对炼油行业提出了难题。重油中硫、氮、金属等杂质含量多,不利于对后续产品的加工,因而必须进行处理。工业中通常采用催化剂加氢以处理重油,在已有的加氢技术中,固定床加氢工艺投资较小,但催化剂易因局部过热而失活,悬浮床加氢反应器虽然存在一些技术缺陷,但其操作方便、热量传递效率高,极大地延长了催化剂寿命,而且可以加工稠油原料。负载型悬浮床加氢催化剂中,催化剂催化活性的主要来源是负载于氧化铝载体上的选自第VIB族和VIII族的活性金属组分,可以促进氢分子的活化、烃分子的氢解以及脱硫脱氮等反应。载体的酸性对催化剂性能影响较大,采用引入酸性组分的手段来调变催化剂载体的酸性,有助于提高催化剂的加氢活性。
中国专利CN1040610A公开了一种以含有氧化钛的γ-氧化铝为载体,W-Mo-Ni为活性组分的烃类加氢精制催化剂。利用氧化钛改性氧化铝载体能在一定程度上改进催化剂的性能,但载体酸量较低,不利于氮杂环的开环断裂。当加工处理氮含量较高的原料时,脱氮效果不明显,不利于催化剂长期运转活性。
中国专利CN106925285A公开了一种以层状黏土和含硅的氧化铝为载体,以W、Ni、Mo、Co为活性组分的重油加氢催化剂,采用饱和喷浸法制备,将活性金属溶液喷浸到载体上。中国专利CN105749925A公开了一种重油加氢催化剂,含硅或氟的氧化铝载体在密闭条件下进行水热处理,然后通过浸渍的方式将金属组分钼以及镍、钴负载到载体上,所得催化剂用于重油加氢处理时有较好的脱硫、脱氮和脱残炭效果。但是,采用常规浸渍法在载体上负载金属,受浸渍液浓度的限制,制备的催化剂不易具有较高的活性金属含量和金属分散度,影响催化剂的活性提高。
美国专利US6387248采用干混捏法制备重油加氢催化剂,在酸(磷酸、硝酸或乙酸)的存在下将多孔氧化铝载体与第VIB、VIII族金属的盐进行研磨,然后再挤出、干燥、焙烧。由于金属组分是以金属盐粉末的形式加入到氧化铝粉中,容易造成活性金属在载体上分布不均匀。
另外,以上技术提供的这些催化剂亲油性较差,用于重油悬浮床加氢处理时,催化剂的分散工艺较复杂,能耗高。
发明内容
针对上述现有技术存在的不足,本发明的目的是提供一种新的表面酸性适中、活性金属分散均匀,加氢脱硫、脱氮、裂化效果好的加氢催化剂及其制备方法,本发明还提供了上述催化剂在油相中分散的重油悬浮床加氢处理中的应用。
本发明是在铝盐的水解液中加入含硅源的水溶液,易于调节催化剂的表面酸性。在载体SiO2-AlOOH的合成过程中加入活性金属盐,可以得到活性金属含量很高的催化剂,并且活性金属在载体上分散均匀。催化剂前驱体在油相中进行热处理,形成的催化剂具有亲油性,用于悬浮床加氢处理时,容易在重油中均匀分散。
本发明提供了一种加氢催化剂,包括载体、钼和至少一种选自第VIII族的活性金属组分。
上述的加氢催化剂中,以氧化物计并以催化剂为基准,金属组分钼含量为5-45重量%,第VIII族的金属组分含量为0.1-10重量%,载体含量为45-92重量%,SiO2占载体的重量百分比为2-50%,其中所述第VIII族的金属组分为镍或钴。所得催化剂的≥350℃红外总酸量为40-350μmol/g,B酸/L酸的比例是0.5-3.2,所述载体是SiO2-AlOOH复合物,所述催化剂采用XRD表征时,具有AlOOH的结构,且在2θ=26o时没有出现MoO3特征峰。
本发明提供了上述加氢催化剂的制备方法,包括以下步骤:
a) 在铝盐的水解液中加入含硅源的水溶液,于60-90 ℃温度范围内搅拌1-4 小时,所述水解液中水/铝摩尔比为50:1~150:1,硅源溶液的浓度为20重量%~50重量%(以SiO2计),所述铝盐为硝酸铝、氯化铝、硫酸铝或异丙醇铝中的一种,硅源选自正硅酸甲酯、正硅酸乙酯、正硅酸丙酯或硅溶胶中的至少一种;
b) 将含金属组分钼和至少一种选自第VIII族的加氢活性金属组分的化合物的水溶液加入步骤a) 制备的反应混合物中,然后在60-100 ℃温度范围内搅拌1-10 小时,制得催化剂前驱体;
c) 将步骤b) 制备的前驱体进行老化、液相热处理后得到催化剂,所述老化温度为20-100 ℃,老化时间为3小时-7天,所述液相热处理溶剂为液体石蜡,热处理温度为200-400℃,热处理时间为2-8 小时,热处理压力为常压-5 MPa。
本发明提供了上述加氢催化剂在重油悬浮床加氢处理中的应用。所述重油选自催化裂化油浆、煤焦油、深拔蜡油、常压渣油或减压渣油中的至少一种。
在重油悬浮床加氢处理条件下,将重油、氢气与加氢催化剂接触并进行重油悬浮床加氢处理;在连续反应装置中,重油悬浮床加氢处理的条件为:反应温度为350-480℃,反应压力为5-16MPa,体积空速0.1-4小时-1,氢油体积比为200-2000;催化剂加入量以金属氧化物计为0.1wt%-1.5wt%。
将重油、氢气与加氢催化剂接触并进行重油悬浮床加氢处理;在间歇反应装置中,重油悬浮床加氢处理的条件为:反应温度为350-450℃,反应压力为5-16MPa,反应时间1~6小时;催化剂加入量以金属氧化物计为0.3wt%-2wt%。
本发明的有益效果:
本发明在铝盐的水解液中加入含硅源的水溶液,催化剂的表面酸性易于调节;在载体SiO2-AlOOH的合成过程中加入活性金属盐,可以得到活性金属含量很高的催化剂,并且活性金属在载体上分散均匀;合成的催化剂具有亲油性,容易在重油中均匀分散;与现有重油加氢处理催化剂相比,采用本发明的加氢催化剂进行重油悬浮床加氢处理,能够获得更好的加氢脱硫、脱氮和裂化效果。
附图说明
图1是本发明实施例1所制备的加氢催化剂C-1的XRD谱图。
具体实施方式
下面将通过实施例对本发明进行进一步的说明,但是并不因此而限制本发明。下述实施例仅为本发明的优选技术方案,并不用于对本发明进行任何限制。对于本领域技术人员而言,本发明可以有各种更改和变化。凡在本发明的精神和原则之内,所作的任何修改、等同替换、改进等,均应包含在本发明的保护范围之内。
根据本发明,X射线衍射(XRD)的晶相图是用Shimadzu XRD7000 X测定得到,测试条件为:Cu靶,Kα辐射,Ni滤波片,超能探测器,管电压40KV,管电流40mA。
实施例1-6说明本发明提供的加氢催化剂及其制备方法。
实施例1
称取21.1g异丙醇铝,均匀分散在150g去离子水中制成浆液,然后加入5.2g 30%硅溶胶,于85℃下反应2小时后得混合物A。称取四水合钼酸铵2.2g,六水合硝酸镍1.8g,分别与10mL去离子水配制成溶液,依次加入到混合物A中,在90℃反应6小时后即可得到催化剂前驱体。
催化剂前驱体于25℃下老化处理7天,然后分散于液体石蜡中,并在320℃、常压下热处理5小时,得到催化剂C-1。
催化剂C-1的XRD表征结果如图1所示,呈现AlOOH的特征衍射峰。在2θ=26o时没有出现MoO3和NiO的特征峰,说明负载的活性金属在载体表面分散良好,没有明显聚集现象。
实施例2
称取23.3g异丙醇铝,均匀分散在165g去离子水中制成浆液,然后加入1.5g正硅酸乙酯,于85℃下反应2小时后得混合物A。称取四水合钼酸铵2.2g,六水合硝酸镍3.6g,分别与5mL去离子水配制成溶液,依次加入到混合物A中,在90℃反应6小时后即可得到催化剂前驱体。
催化剂前驱体于40℃下老化处理5天,然后分散于液体石蜡中,并在280℃、常压下热处理8小时,得到催化剂C-2。
实施例3
称取17.6g异丙醇铝,均匀分散在130g去离子水中制成浆液,然后加入7.0g 40%硅溶胶,于85℃下反应2小时后得混合物A。称取四水合钼酸铵2.2g,六水合硝酸镍0.9g,分别与5mL去离子水配制成溶液,依次加入到混合物A中,在90℃反应6小时后即可得到催化剂前驱体。
催化剂前驱体于70℃下老化处理2天,然后分散于液体石蜡中,并在280℃、常压下热处理8小时,得到催化剂C-3。
实施例4
称取40.7g九水合硝酸铝,130g去离子水中制成浆液,然后加入2.5g正硅酸乙酯,于90℃下反应3小时后得混合物A。称取四水合钼酸铵2.7g,六水合硝酸镍2.2g,分别与10mL去离子水配制成溶液,依次加入到混合物A中,在90℃反应4小时后即可得到催化剂前驱体。
催化剂前驱体于40℃下老化处理5天,然后分散于液体石蜡中,并在280℃、常压下热处理4小时,得到催化剂C-4。
实施例5
称取12.2g氯化铝,均匀分散在75g去离子水中制成浆液然后加入4.6g 40%硅溶胶,于90℃下反应3小时后得混合物A。称取四水合钼酸铵3.1g,六水合硝酸钴2.5g,分别与10mL去离子水配制成溶液,依次加入到混合物A中,在90℃反应4小时后即可得到催化剂前驱体。
催化剂前驱体于70℃下老化处理2天,然后分散于液体石蜡中,并在350℃、3MPa下热处理4小时,得到催化剂C-5。
实施例6
称取13.6g氯化铝,均匀分散在101g去离子水中制成浆液然后加入3.7g正硅酸乙酯,于90℃下反应3小时后得混合物A。称取四水合钼酸铵3.1g,六水合硝酸钴1.3g,分别与10mL去离子水配制成溶液,依次加入到混合物A中,在90℃反应4小时后即可得到催化剂前驱体。
催化剂前驱体于40℃下老化处理5天,然后分散于液体石蜡中,并在310℃、常压下热处理4小时,得到催化剂C-6。
对比例1-3说明对比催化剂的制备方法。
对比例1
制备得到催化剂R-1(载体中不含SiO2),其余条件与实施例1完全相同。
称取26.3g异丙醇铝,均匀分散在150g去离子水中制成浆液,于85℃下反应2小时后得混合物A。称取四水合钼酸铵2.2g,六水合硝酸镍1.8g,分别与10mL去离子水配制成溶液,依次加入到混合物A中,在90℃反应6小时后即可得到催化剂前驱体。
催化剂前驱体于25℃下老化处理7天,然后分散于液体石蜡中,并在320℃、常压下热处理5小时,得到催化剂R-1。
对比例2
制备得到催化剂R-2(浸渍法制备催化剂NiMo/γ-Al2O3),NiMo负载量与对比例中R-1相同。
称取2.2g四水合钼酸铵和1.8g六水合硝酸镍,分别用稀氨水溶液溶解,再混合均匀。用配制的含活性金属的稀氨水溶液等体积浸渍7.7g工业载体γ-氧化铝,室温过夜后,置于110℃干燥12小时,然后于450℃下焙烧4小时,得到催化剂R-2。
对比例3
制备得到催化剂R-3(浸渍法制备催化剂NiMo/SiO2-Al2O3,载体中含20%SiO2),NiMo负载量与对比例中R-1相同。
称取2.2g四水合钼酸铵和1.8g六水合硝酸镍,分别用稀氨水溶液溶解,再混合均匀。用配制的含活性金属的稀氨水溶液等体积浸渍7.7g含20%SiO2的氧化铝载体,室温过夜后,置于110℃干燥12小时,然后于450℃下焙烧4小时,得到催化剂R-3。
实施例7-12说明本发明提供的催化剂(实施例1-6所得催化剂)在重油加氢处理中的应用。
以硫含量为0.32%、氮含量为0.28%的催化裂化油浆为反应原料,在100mL高压加氢反应釜中评价催化剂C-1、C-2、C-3、C-4、C-5、C-6的加氢脱硫、脱氮、裂化活性。将40g催化裂化油浆、0.5g硫粉和1.2g催化剂加入反应釜中,充分混合。反应条件为:反应温度380℃,氢气压力为12MPa,反应时间为4小时。反应结束后,快速冷却至室温。使用紫外荧光硫测定仪分析加氢产物油的硫含量,使用化学发光定氮仪分析加氢产物油的氮含量,使用模拟蒸馏仪测定原料油和加氢产物油的馏程分布。按照下列公式分别计算脱硫率XS和脱氮率XN:
其中,FS为原料油中的硫含量,PS为产物油中的硫含量;FN为原料油中的氮含量,PN为产物油中的氮含量。
实验结果见表1和表2。
对比例4-6说明对比催化剂(对比例1-3所得催化剂)的性能。
按照与实施例7完全相同方法评价催化剂R-1、R-2和R-3,结果如表1和表2所示。
表1 加氢反应结果
表2 原料油和产物油的馏程分布
对比催化剂R-1不含SiO2,其余制备条件与实施例1中C-1完全相同,对比催化剂R-2是采用浸渍法制备的NiMo/γ-Al2O3(工业载体),Ni、Mo负载量与对比例中R-1相同,对比催化剂R-3是采用浸渍法制备的催化剂NiMo/SiO2-Al2O3,Ni、Mo负载量与对比例中R-1相同,但SiO2-Al2O3-载体中含有20%SiO2。从表1和表2中的数据可以看出,催化剂C-1、C-2、C-3、C-4、C-5和C-6的脱硫率、脱氮率均高于对比催化剂R-1、R-2和R-3。表明采用本发明的加氢催化剂进行重油悬浮床加氢处理时,能够获得更好的加氢脱硫、脱氮和裂化效果。
Claims (10)
1.一种加氢催化剂,其特征在于:包括载体、钼和至少一种选自第VIII族的活性金属组分,所述载体是SiO2-AlOOH复合物;在载体SiO2-AlOOH的合成过程中加入活性金属盐,使得最终形成的催化剂中活性金属在载体上均匀分散。
2.根据权利要求1所述的加氢催化剂,其特征在于:以氧化物计并以催化剂为基准,金属组分钼含量为5-45重量%,第VIII族的金属组分含量为0.1-10重量%,载体含量为45-92重量%,SiO2占载体的重量百分比为2-50%,其中所述第VIII族的金属组分为镍或钴。
3.根据权利要求1所述的加氢催化剂,其特征在于:所得催化剂的≥350℃红外总酸量为40-350μmol/g,B酸/L酸的摩尔比是0.5-3.2,所述载体是SiO2-AlOOH复合物,所述催化剂采用XRD表征时,具有AlOOH的结构。
4.一种权利要求1~3任一项所述的加氢催化剂的制备方法,其特征在于包括以下步骤:
a) 在铝盐的水解液中加入含硅源的水溶液,于60-90 ℃温度范围内搅拌1-4 小时;
b) 将含金属组分钼和至少一种选自第VIII族的加氢活性金属组分的化合物的水溶液加入步骤a) 制备的反应混合物中,然后在60-100 ℃温度范围内搅拌1-10 小时,制得催化剂前驱体;
c) 将步骤b) 制备的前驱体进行老化、液相热处理后得到催化剂。
5.根据权利要求4所述的加氢催化剂的制备方法,其特征在于:步骤a)中,所述水解液中水/铝摩尔比为50:1~150:1;以SiO2计,硅源溶液的浓度为20重量%~50重量%;所述铝盐为硝酸铝、氯化铝、硫酸铝或异丙醇铝中的一种,硅源选自正硅酸甲酯、正硅酸乙酯、正硅酸丙酯或硅溶胶中的至少一种。
6.根据权利要求4所述的加氢催化剂的制备方法,其特征在于:步骤c)中,所述老化温度为20-100 ℃,老化时间为3小时-7天。
7.根据权利要求4所述的加氢催化剂的制备方法,其特征在于:步骤c)中,所述液相热处理溶剂为液体石蜡,热处理温度为200-400 ℃,热处理时间为2-8 小时,热处理压力为常压-5 MPa。
8.一种权利要求1~3任一项所述的加氢催化剂在重油悬浮床加氢处理中的应用,其特征在于: 所述重油选自催化裂化油浆、煤焦油、深拔蜡油、常压渣油或减压渣油中的至少一种。
9.根据权利要求8所述的应用,其特征在于:在重油悬浮床加氢处理条件下,将重油、氢气与加氢催化剂接触并进行重油悬浮床加氢处理;在连续反应装置中,重油悬浮床加氢处理的条件为:反应温度为350-480℃,反应压力为5-16MPa,体积空速0.1-4小时-1,氢油体积比为200-2000;催化剂加入量以金属氧化物计为0.1wt%-1.5wt%。
10.根据权利要求8所述的应用,其特征在于:将重油、氢气与加氢催化剂接触并进行重油悬浮床加氢处理;在间歇反应装置中,重油悬浮床加氢处理的条件为:反应温度为350-450℃,反应压力为5-16MPa,反应时间1~6小时;催化剂加入量以金属氧化物计为0.3wt%-2wt%。
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