CN1854261A - 一种加氢裂化催化剂组合物 - Google Patents

一种加氢裂化催化剂组合物 Download PDF

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CN1854261A
CN1854261A CNA2005100681738A CN200510068173A CN1854261A CN 1854261 A CN1854261 A CN 1854261A CN A2005100681738 A CNA2005100681738 A CN A2005100681738A CN 200510068173 A CN200510068173 A CN 200510068173A CN 1854261 A CN1854261 A CN 1854261A
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aluminum oxide
pore volume
organic
organism
content
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CN100425676C (zh
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毛以朝
聂红
董建伟
熊震霖
胡志海
石亚华
李大东
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Sinopec Research Institute of Petroleum Processing
China Petroleum and Chemical Corp
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Sinopec Research Institute of Petroleum Processing
China Petroleum and Chemical Corp
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Priority to CNB2005100681738A priority Critical patent/CN100425676C/zh
Application filed by Sinopec Research Institute of Petroleum Processing, China Petroleum and Chemical Corp filed Critical Sinopec Research Institute of Petroleum Processing
Priority to CA2592332A priority patent/CA2592332C/en
Priority to KR1020137012243A priority patent/KR20130060367A/ko
Priority to PCT/CN2006/000798 priority patent/WO2006116913A1/zh
Priority to US11/912,566 priority patent/US20080190811A1/en
Priority to EP06741727.9A priority patent/EP1875962B1/en
Priority to KR1020077015920A priority patent/KR101446658B1/ko
Publication of CN1854261A publication Critical patent/CN1854261A/zh
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Publication of CN100425676C publication Critical patent/CN100425676C/zh
Priority to US12/960,159 priority patent/US8883669B2/en
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Abstract

一种加氢裂化催化剂组合物，该组合物由一种酸性硅铝、有效量的至少一种第VIII族和至少一种第VIB族的金属组分及有机添加物组成，其中的有机物选自含氧或含氮的有机物中的一种或几种，有机物与第VIII族金属组分的摩尔比为0.01－10。该催化剂用于加氢裂化过程中，具有更高的芳烃加氢饱和及开环活性。

Description

一种加氢裂化催化剂组合物
                             技术领域
本发明是关于一种加氢裂化催化剂组合物。
                            背景技术
加氢裂化催化剂是一种双功能催化剂，它同时具有裂解活性和加氢活性，即同时含有酸性组分和加氢活性组分；裂化组分一般选自酸性硅铝，包括：氧化硅-氧化铝、沸石分子筛及其混合物，加氢活性组分一般选自元素周期表中VIB族和VIII族的金属、金属氧化物和/或金属硫化物。为达到对加氢裂解产物的不同要求，需要对催化剂中的酸性组分和加氢活性组分进行适应性调变。
CN1054150C公开了一种柴油加氢转化催化剂，该催化剂由氧化铝、无定形硅铝及分子筛组成的载体及负载在该载体上的加氢活性金属组成，催化剂中WO3的含量为10-30重％、NiO的含量为2-15重％、分子筛的含量为5-45重％、氧化铝的含量为30-70重％、无定形硅铝的含量为5-25重％，所述分子筛为Y型分子筛，其红外总酸量为0.5-1毫摩尔/克，晶胞常数为2.436-2.444纳米。所述氧化铝为孔容0.8-1.1毫升/克；表面积230-400米2/克的小孔氧化铝。
CN1184843A公开了一种柴油加氢转化催化剂，该催化剂的组成为氧化铝40-80重％、无定形硅铝0-20重％、分子筛5-30重％，所述分子筛为孔容0.40-0.52毫升/克，比表面750-900米2/克，晶胞常数2.420-2.500，硅铝比7-15的Y型分子筛，VIB族金属含量10-30重％，Vlll族金属氧化物的含量为2-15重％。
US5,030,780公开了一种芳烃化合物的饱和方法，该方法使用了一种催化剂，所述催化剂含有负载在一种载体上的加氢金属，所述催化剂载体含有一种沸石与一种多孔耐热无机氧化物，特别是含有分散在氧化铝基质中的硅-铝的耐热无机氧化物，所述沸石包括已知的自然或人工合成的各种结晶硅铝沸石，如八面沸石、丝光沸石、erionite沸石、Y型沸石、X型沸石、L沸石、Ω沸石、ZSM-4沸石、Beta沸石等。
CN1055961C公开了一种特别适用于生产中间馏分油的加氢裂化催化剂，含有无定形硅铝组分和小孔氧化铝粘合剂，无定形硅铝的含量为30-60w％，至少一种VIB族元素和至少一种VIII族元素，加氢金属氧化物总含量为20-35w％，余量为小孔氧化铝粘合剂，其特征在于催化剂比表面150-300m2/g，孔容0.25-0.50ml/g，4-15nm孔分布在60-90％，红外酸度0.30-0.50mmol/g。
CN1400284A公开了一种柴油加氢处理催化剂，该催化剂含有一种载体和负载在该载体上的钼和/或钨及镍和/或钴，其特征在于，所述载体由氧化铝和沸石组成，氧化铝与沸石的重量比为90∶10-50∶50，所述氧化铝是由小孔氧化铝和大孔氧化铝按照75∶25-50∶50的重量比复合而成的氧化铝，其中，小孔氧化铝为直径小于80埃孔的孔体积占总孔体积95％以上的氧化铝，大孔氧化铝为直径60-600埃孔的孔体积占总孔体积70％以上的氧化铝。
现有技术提供的加氢裂化催化剂可满足一些加氢裂化反应的要求，但普遍存在的问题是芳烃加氢转化活性低。
                            发明内容
本发明的目的是克服现有加氢裂化催化剂芳烃加氢转化活性低的缺点，提供一种新的芳烃加氢转化活性高的加氢裂化催化剂组合物及其制备方法。
本发明提供的催化剂组合物由一种酸性硅铝、有效量的至少一种第VIII族和至少一种第VIB族的金属组分及有机添加物组成，其中的有机物选自含氧或含氮的有机物中的一种或几种，有机物与第VIII族金属组分的摩尔比为0.01-10。
本发明提供催化剂组合物的制备方法包括向一种酸性硅铝引入有效量的至少一种第VIII族和至少一种第VIB族金属组分及有机添加物，其中的有机物选自含氧或含氮的有机物中的一种或几种，有机物的引入量使所述催化剂组合物中有机物与第VIII族金属组分的摩尔比为0.01-10。
与现有技术相比，本发明提供的催化剂组合物的芳烃加氢转化活性得到显著提高。
例如，在相同反应条件下，采用含四氢萘5.61％的正辛烷溶液评价本发明提供的催化剂组合物C-1，其芳烃加氢转化活性为12.3％；而参比催化剂RC-1的芳烃加氢转化活性仅为9.1。
                          具体实施方式
按照本发明提供的催化剂组合物，其中所述的有机物与第VIII族金属组分的摩尔比优选为0.05-8。
按照本发明提供的催化剂组合物，其中所述的酸性硅铝可以是选自常用作裂化活性组分的氧化硅-氧化铝、硅铝酸盐、沸石分子筛中的一种或几种；可以是氧化硅-氧化铝、硅铝酸盐、沸石分子筛中的一种或几种与常作为催化剂基质的耐热无机氧化物的混合物。其中，所述的沸石可以是具有大孔结构的沸石，如具有八面沸石、Beta沸石、Ω沸石结构的沸石，可以是具有中孔结构的沸石，如具有丝光沸石、ZSM-5沸石、ZSM-11沸石、ZSM-22沸石、ZSM-23沸石、ZSM-35沸石、ZSM-48沸石、ZSM-57沸石等结构的沸石，也可以是具有小孔结构的沸石，如具有Erionite沸石、ZSM-34沸石结构的沸石。优选具有八面沸石结构的沸石、具有Beta沸石结构的沸石、具有ZSM-5结构的沸石、具有丝光沸石结构的沸石中的一种或几种。所述具有八面沸石结构的沸石优选为Y型沸石，进一步优选其中的HY沸石、稀土型Y沸石REY、稀土型HY沸石REHY、超稳Y沸石USY、稀土型超稳Y沸石REUSY、含磷的Y及超稳及HY型沸石、脱铝Y型沸石中的一种或几种。所述耐热无机氧化物选自氧化铝、氧化硅、氧化钛、氧化镁、氧化铝-氧化镁、氧化硅-氧化镁、氧化硅-氧化锆、氧化硅-氧化钍、氧化硅-氧化铍、氧化硅-氧化钛、氧化硅-氧化锆、氧化钛-氧化锆、氧化硅-氧化铝-氧化钍、氧化硅-氧化铝-氧化钛、氧化硅-氧化铝-氧化镁、氧化硅-氧化铝-氧化锆、粘土中的一种或几种，优选氧化铝，进一步优选的氧化铝包括一种孔直径为径60-600埃孔的孔体积占总孔体积70％以上的氧化铝。更为优选以氧化铝的总量为基准，所述氧化铝中的直径60-600埃孔的孔体积占总孔体积70％以上氧化铝的含量至少为50重量％。
当所述酸性硅铝为氧化硅-氧化铝、硅铝酸盐、沸石分子筛中的一种或几种与耐热无机氧化物的混合物时，以所述混合物重量为基准，优选耐热无机氧化物的含量为20-95重量％，所述氧化硅-氧化铝、硅铝酸盐、沸石分子筛中的一种或几种的含量为5-80重量％。
按照本发明提供的催化剂，所述的第VIII族金属组分优选为钴和/或镍，第VIB族金属组分优选为钼和/或钨。以氧化物计并以催化剂为基准，第VIII族金属组分的含量优选为1-10重量％，进一步优选为2-8重量％，第VIB族金属组分的含量优选为5-40重量％，进一步优选为10-35重量％。
按照本发明提供的方法，所述引入至少一种第VIII族和至少一种第VIB族金属组分及有机物的方法，可以是将有机物与含有至少一种第VIII族和至少一种选自第VIB族金属化合物配制成混合溶液后与所述的酸性硅铝接触，如通过浸渍的方法；可以是将含有至少一种第VIII族和至少一种选自第VIB族金属化合物及有机物单独配制溶液后与所述的酸性硅铝接触，如通过浸渍的方法。所述的浸渍方法为常规方法，通过对含至少一种第VIII族和至少一种第VIB族金属组分及有机化合物中一种或几种的溶液的浓度、用量或酸性硅铝用量的调节和控制，制备指定加氢金属及有机添加物含量催化剂的方法为本领域技术人员所公知。
当有机物与第VIII族和第VIB族金属组分同时引入所述酸性硅铝时，优选包括干燥的步骤；当有机物与第VIII族和第VIB族金属组分分别引入所述酸性硅铝时，优选首先用含有至少一种第VIII族和至少一种第VIB族的金属化合物的溶液与该酸性硅铝接触、干燥、焙烧或不焙烧，之后再与含有机物的溶液接触并干燥。所述干燥和焙烧的条件为制备催化剂惯用的条件，如干燥温度为80-350℃，优选为100-300℃，干燥时间为1-24小时，优选为2-12小时，焙烧温度为350-550℃优选为400-500℃，焙烧时间为1-10小时，优选为2-8小时。所述有机物的引入量优选使最终催化剂中有机物与第VIII族金属组分的摩尔比为0.05-8。
所述第VIII族金属化合物选自这些金属的可溶性化合物中的一种或几种，例如，可以是这些金属的硝酸盐、醋酸盐、碳酸盐、氯化物、可溶性络合物中的一种或几种。
所说的第VIB族金属化合物选自这些金属的可溶性化合物中的一种或几种，例如，可以是钼酸盐、仲钼酸盐、钨酸盐、偏钨酸盐、乙基偏钨酸盐中的一种或几种。
所述有机物可以是含氧和/或含氮的有机物的一种或几种。如含氧有机化合物可以是有机醇、有机酸中的一种或几种，含氮有机化合物可以是有机胺中的一种或几种。优选的含氧化合物可以是乙二醇、丙三醇、聚乙二醇(分子量为200-1500)、乙酸、马来酸、草酸、氨基三乙酸、1，2-环己烷二胺四乙酸、柠檬酸中的一种或几种，含氮有机化合物可以是乙二胺或EDTA。
按照本发明提供的催化剂，视不同目的或要求可制成各种易于操作的成型物，例如微球、球形、片剂或条形等。成型可按常规方法进行，如压片、滚球、挤条等方法均可。
按照本领域中的常规方法，本发明提供的催化剂在使用之前，通常可在氢气存在下，于140-370℃的温度下用硫、硫化氢或含硫原料进行预硫化，这种预硫化可在器外进行也可在器内原位硫化，将其转化为硫化物型。
本发明提供的催化剂适用于对烃类原料进行加氢裂化，以生产具有较低沸点和较低分子量的烃类馏分和低芳烃含量的加氢裂化尾油。所述烃类原料可以是各种重质矿物油或合成油或它们的混合馏分油，如直馏瓦斯油(straightrun gas oil)、减压瓦斯油(vacuum gaso il)、脱金属油(demetallizedoils)、常压渣油(atmospheric residue)、脱沥青减压渣油(deasphaltedvacuum residue)、焦化馏出油(coker distillates)、催化裂化馏出油(catcraker distillates)、页岩油(shale oil)、沥青砂油(tar sand oil)、煤液化油(coal liquid)等。本发明提供的催化剂特别适用于重质和劣质馏分油的加氢裂化过程，尤其适用于生产馏程为370-520℃低芳烃含量的加氢裂化尾油馏分的加氢裂化过程。
本发明提供的催化剂用于馏分油加氢裂化时，可在常规的加氢裂化工艺条件下使用，如反应温度200-650℃，优选300-510℃，反应压力3-24兆帕，优选4-15兆帕，液时空速0.1-10小时-1优选0.2-5小时-1，氢油体积比100-5000，优选200-1000。
下面将通过实例说明本发明。
实例中所用试剂，除特别说明的以外，均为化学纯试剂。
实例1
将80克PSRY沸石(长岭催化剂厂生产，晶胞常数24.50～24.60，含磷0.5～2.0，商品名PSRY)同920克干基拟薄水铝石(山东铝厂生产，直径小于80埃孔的孔体积占总孔体积95％以上，商品名SD粉)(均以干基计，下同)，30克田菁粉混合，挤成外接圆直径为1.6毫米的三叶形条，120℃烘干，600℃温度下焙烧3小时，得载体CS-1，催化剂载体组成见表1。取100g载体CS-1用含仲钼酸铵(株洲硬质合金厂，氧化钼含量为80重量％)6.76克、硝酸钴(北京化工厂产品，氧化钴含量为24.5重量％)22克、EDTA1.05克的70ml含氨水溶液浸渍，220℃处理1小时，得到催化剂C-1，其组成见表2。
对比例1
取100g CS-1载体用含仲钼酸铵(株洲硬质合金厂，氧化钼含量为80重量％)6.76克、硝酸钴(北京化工厂产品，氧化钴含量为24.5重量％)22克的70ml含氨水溶液浸渍，120℃烘干，在480℃焙烧4小时，得到催化剂RC-1，其组成见表2。
实例2
将800克SiAl粉(德国SASOL生产，商品名Siral-40)同200克干基拟薄水铝石(山东铝厂生产，直径小于80埃孔的孔体积占总孔体积95％以上，商品名SD粉)，挤成外接圆直径为1.2毫米的圆柱形条，120℃烘干，500℃温度下焙烧3小时，得载体CS-2，催化剂载体组成见表1。降温至室温后，取100g CS-2载体用含偏钨酸铵(四川自贡硬质合金厂，氧化钨含量为82重量％)38.25克、硝酸镍(北京益利精细化学品有限公司产品，氧化镍含量为25.4重量％)24.37克的85ml水溶液浸渍，180℃处理4小时，降温至室温后用39.04克乙二醇浸渍，105℃处理10小时，得到催化剂C-2，其组成见表2。
实例3
将300克SiAl粉(德国SASOL生产，商品名Siral-40)同300克干基氢氧化铝粉(长岭催化剂厂生产，直径60-600埃孔的孔体积占总孔体积70％以上，商品名CL干胶粉)，挤成外接圆直径为1.2毫米的圆柱形条，120℃烘干，500℃温度下焙烧3小时，得载体CS-3，催化剂载体组成见表1。降温至室温后，取100g CS-3载体用含偏钨酸铵(四川自贡硬质合金厂，氧化钨含量为82重量％)38.25克、硝酸镍(北京益利精细化学品有限公司产品，氧化镍含量为25.4重量％)24.37克的85ml水溶液浸渍，180℃处理4小时，降温至室温后用39.04克乙二醇浸渍，105℃处理10小时，得到催化剂C-3，其组成见表2。
实例4
将800克SiAl粉(德国SASOL生产，商品名Siral-40)同200克干基氢氧化铝粉(长岭催化剂厂生产，直径60-600埃孔的孔体积占总孔体积70％以上，商品名CL干胶粉)，100克干基拟薄水铝石(山东铝厂生产，直径小于80埃孔的孔体积占总孔体积95％以上，商品名SD粉)，300克干基超稳Y型分子筛(长岭催化剂厂生产，晶胞常数24.55，商品名LAY)，挤成外接圆直径为1.5毫米的蝶型条，120℃烘干，550℃温度下焙烧3小时，得载体CS-4，催化剂载体组成见表1。降温至室温后，取100g CS-4载体用含乙二胺1.78克的70ml水溶液浸渍，80℃处理24小时，再用含偏钨酸铵(四川自贡硬质合金厂，氧化钨含量为82重量％)54.84克、硝酸镍(北京益利精细化学品有限公司产品，氧化镍含量为25.4重量％)17.35克的70ml水溶液浸渍，100℃处理4小时，降温至室温后得到催化剂C-4，其组成见表2。
实例5
将450克干基氢氧化铝粉(长岭催化剂厂生产，直径60-600埃孔的孔体积占总孔体积70％以上，商品名CL干胶粉)，350克干基拟薄水铝石(山东铝厂生产，直径小于80埃孔的孔体积占总孔体积95％以上，商品名SD粉)，100克干基ZSM-5分子筛(长岭建长催化剂厂生产，硅铝比50)，100克干基Beta分子筛(长岭建长催化剂厂生产，硅铝比27)，挤成外接圆直径为3.6毫米的蝶型条，120℃烘干，550℃温度下焙烧3小时，得载体CS-5，催化剂载体组成见表1。降温至室温后，取100g CS-5载体用含仲钼酸铵(株洲硬质合金厂，氧化钼含量为80重量％)9.25克，偏钨酸铵(四川自贡硬质合金厂，氧化钨含量为82重量％)43.84克、硝酸镍(北京益利精细化学品有限公司产品，氧化镍含量为25.4重量％)18.05克的80ml水溶液浸渍，120℃干燥，450℃焙烧3hr。降温至室温后，用含柠檬酸26.41克的50ml水溶液浸渍，120℃干燥4hr得到催化剂C-5，其组成见表2。
表1
实例 载体编号   氧化铝，重量％   硅铝，重量％
  SD粉   CL粉   SiAl粉   沸石
  1   CS-1   92   8
  2   CS-2   20   80
  3   CS-3   20   80
  4   CS-4   10   30   30   30
  5   CS-5   35   45   20
表2
实例   催化剂编号   VIII族金属，重量％   VIB族金属，重量％   有机物，
  NiO   CoO   WO3   MoO3   mol/mol*
 1   C-1   4.4   14.2   0.05
 对比例1   RC-1   4.4   14.2
 2   C-2   4.5   22.8   7.6
 3   C-3   4.5   22.8   7.6
 4   C-4   2.95   30.1   0.5
 5   C-5   3.1   24.3   5   2.2
*：有机物摩尔比指催化剂中有机物同VIII族金属的摩尔比。
实例6～10
本实例说明本发明催化剂C1-C5的催化效果。
在2ml加氢裂化装置上评价催化剂C1-C5的加氢裂化活性，催化剂装量为0.2毫升，催化剂颗粒直径为0.3-0.45毫米，反应温度390℃，反应压力4.0兆帕，氢油比(摩尔比)为25，液时空速为30小时-1，用含四氢萘5.61％的正辛烷溶液进行微反评价，催化剂进反应油前进行硫化，硫化条件为：在氢气压力2.0MPa的条件下，升温至60℃，通入含6％CS2的正己烷溶液，升温至300℃，恒温4hr。
以下式定义催化剂的芳烃加氢转化活性：
芳烃加氢转化活性＝100-(产物中四氢萘总量+产物中萘总量)/原料中四氢萘总量×100。
结果见表3。
对比例2
采用实例6的方法进行RC-1催化剂的评价。结果见表3。
表3
  实例   催化剂   芳烃加氢转化活性
  对比例2   RC-1   9.1
  6   C-1   12.3
  7   C-2   11.1
  8   C-3   13.5
  9   C-4   75.3
  10   C-5   62.4
由表3可知，采用有机添加物后，C-1催化剂的芳烃加氢转化活性明显提高，相对于未采用添加物的催化剂RC-1提高3.2％，而同时采用直径60-600埃孔的孔体积占总孔体积70％以上的大孔氧化铝制备的催化剂C-3，相对于直径小于80埃孔的孔体积占总孔体积95％以上的小孔氧化铝制备的催化剂C-2，其芳烃加氢转化活性得到进一步的提高，提高2.4％。

Claims (12)

1、一种加氢裂化催化剂组合物，该组合物由一种酸性硅铝、有效量的至少一种第VIII族和至少一种第VIB族的金属组分及有机添加物组成，其中的有机物选自含氧或含氮的有机物中的一种或几种，有机物与第VIII族金属组分的摩尔比为0.01-10。
2、按照权利要求1所述的催化剂，其特征在于，所述含氧化合物选自有机醇、有机酸中的一种或几种，含氮有机化合物为有机胺，所述有机物与第VIII族金属组分的摩尔比为0.05-8。
3、按照权利要求1所述的催化剂，其特征在于，所述酸性硅铝选自氧化硅-氧化铝、沸石分子筛中的一种或几种。
4、按照权利要求1所述的催化剂，其特征在于，所述酸性硅铝为氧化硅-氧化铝和/或沸石分子筛与氧化铝的混合物，以所述混合物为基准，氧化铝的含量为20-95，氧化硅-氧化铝和/或沸石分子筛的含量为5-80。
5、按照权利要求4所述的催化剂，其特征在于，所述氧化铝至少包含一种直径60-600埃孔的孔体积占总孔体积70％以上的氧化铝。
6、根据权利要求5所述的催化剂，其特征在于，以氧化铝的总量为基准，所述氧化铝中的直径60-600埃孔的孔体积占总孔体积70％以上氧化铝的含量至少为50重量％。
7、权利要求1所述催化剂组合物的制备方法，该方法包括向一种酸性硅铝引入有效量的至少一种第VIII族和至少一种第VIB族金属组分及有机添加物，其中的有机物选自含氧或含氮的有机物中的一种或几种，有机物的引入量使所述催化剂组合物中有机物与第VIII族金属组分的摩尔比为0.01-10。
8、按照权利要求7所述的方法，其特征在于，所述含氧化合物选自有机醇、有机酸中的一种或几种，含氮有机化合物为有机胺，所述有机物与第VIII族金属组分的摩尔比为0.05-8。
9、按照权利要求7所述的方法，其特征在于，所述酸性硅铝选自氧化硅-氧化铝、沸石分子筛中的一种或几种。
10、按照权利要求7所述的方法，其特征在于，所述酸性硅铝为氧化硅-氧化铝和/或沸石分子筛与氧化铝的混合物，以所述混合物为基准，氧化铝的含量为20-95，氧化硅-氧化铝和/或沸石分子筛的含量为5-80。
11、按照权利要求10所述的方法，其特征在于，所述氧化铝至少包含一种直径60-600埃孔的孔体积占总孔体积70％以上的氧化铝。
12、按照权利要求11所述的方法，其特征在于，以氧化铝的总量为基准，所述氧化铝中的直径60-600埃孔的孔体积占总孔体积70％以上氧化铝的含量至少为50重量％。
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