CN106925279B - 一种Fe系选择加氢催化剂、制备方法及其应用 - Google Patents
一种Fe系选择加氢催化剂、制备方法及其应用 Download PDFInfo
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- CN106925279B CN106925279B CN201511032668.5A CN201511032668A CN106925279B CN 106925279 B CN106925279 B CN 106925279B CN 201511032668 A CN201511032668 A CN 201511032668A CN 106925279 B CN106925279 B CN 106925279B
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- alumina
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Abstract
本发明涉及一种Fe系选择加氢催化剂,催化剂活性组分Fe含量占2~15(wt)%,X含量占0~2(wt)%,X选自K、La、Ce中的一种或者几种。其余为氧元素和载体。催化剂比表面为10~300m2/g,孔容为0.2~0.65ml/g。本发明催化剂可用于C2~3裂解馏分中乙炔、丙炔和丙二烯(MAPD)的选择性加氢。该催化剂具有温和的加氢活性和优异的烯烃选择性,烯烃增量高,操作弹性好,“绿油”生成量低,长周期运行性能好。并且催化剂成本远低于贵金属Pd催化剂。
Description
技术领域
本发明涉及一种Fe系选择加氢催化剂及其制备方法和应用,用于碳二裂解馏分中所含乙炔和丙炔(MA)、丙二烯(PD)选择性加氢制备乙烯、丙烯。
背景技术
乙烯、丙烯是石油化学工业最重要的基础原料之一,作为合成各种聚合物的单体,绝大部分由石油烃(如乙烷、丙烷、丁烷、石脑油和轻柴油等)蒸汽裂解制得。经这种方法得到的以乙烯为主的C2馏分中还含有0.5%~2.5%(摩尔分数)的乙炔。乙炔的存在会使乙烯的聚合过程复杂化,恶化聚合物性能。当用高压法生产聚乙烯时,由于乙炔的积累,会有***的危险;另外,在生产聚乙烯时,乙炔的存在还会降低聚合催化剂活性,增加催化剂的消耗。所以必须将乙烯中的乙炔降到一定值以下,才能作为合成高聚物的单体。
目前工业中通常采用贵金属Pd系加氢催化剂,选择性除去C2馏分中的乙炔和C3馏分中的丙炔(MA)、丙二烯(PD)。专利US4404124通过分步浸渍法制备了活性组分钯壳层分布的选择加氢催化剂,可应用于碳二、碳三馏分的选择加氢,以消除乙烯中的乙炔和丙烯中的丙炔丙二烯。US5587348以氧化铝为载体,调节助催化剂银与钯作用,加入碱金属、化学键合的氟制备了性能优良的碳二加氢催化剂。该催化剂具有减少绿油生成,提高乙烯选择性,减少含氧化合物生成量的特点。US5519566公开了一种湿法还原制备银与钯催化剂的方法,通过在浸渍液中加入有机或无机还原剂,制备银与钯双组分选择加氢催化剂。
由于使用贵金属Pd作为活性组分,催化剂成本居高不下,而且贵金属催化剂由于活性高,在装置开工稳定性,操作弹性和催化剂长周期运行性能方面存在一定问题。研发价格低廉、性能卓越的碳二加氢催化剂体系,一直是该领域科研人员努力的目标。
CN2005800220708.2公布了一种轻质烯烃原料中乙炔和二烯烃的选择加氢催化剂,该催化剂由选自铜、金、银的第一组分和选择镍、铂、钯、铁、钴、钌、铑的第二种组分组成,另外催化剂还包括选自锆、镧系元素和碱土金属混合物的至少一种无机盐和氧化物。催化剂煅烧、使用或者再生后形成萤石结构。催化剂氧化物总含量0.01~50%,优选焙烧温度700~850℃。通过添加第三种氧化物,改性氧化铝或氧化硅载体,有助于增加催化剂选择性和再生之后的活性、选择性。该技术仍旧是以铜、金、银、钯等为活性组分,镍、铂、钯、铁、钴、钌、铑等作为助组分,通过对载体的氧化物改性,提高催化剂的再生性能。
CN102218323A公布了一种不饱和烃的加氢催化剂,活性组分为5~15%的氧化镍和1~10%的其他金属氧化物的混合物,其他金属氧化物可以为氧化钼、氧化钴和氧化铁中的一种或者几种,另外还包括1~10%的助剂。该发明技术主要用于将煤制油工业尾气中乙烯、丙烯、丁烯等加氢转化为饱和烃,具有良好的深度加氢能力。该技术主要用于富含CO和氢气的各种工业尾气中乙烯、丙烯、丁烯等的全加氢,不适合用于炔烃、二烯烃的选择加氢。
ZL201080011940.0公布了一种有序钴-铝和铁-铝间化合物作为乙炔加氢催化剂,所述的金属间化合物选自由CoAl、CoAl3、Co2Al5、Co2Al9、o-Co4Al13、h-Co4Al13、m-Co4Al13、FeAl、FeAl2、Fe3Al、Fe2Al5、Fe4Al13组成的组。其中优选Fe4Al13和o-Co4Al13。所述的金属间化合物采用固态化学中的热熔融法制备得到。在石英管式炉中进行催化剂加氢性能测试,反应温度473K,稳定反应20h后,o-Co4Al13催化剂乙炔转化率达到62%,乙烯选择性达到71%,Fe4Al13催化剂上乙炔转化率达到40%,乙烯选择性达到75%。该技术是在高温条件下制备金属间化合物,用于乙炔的选择性加氢,乙炔转化率低,反应温度高,不利于工业化应用。并且催化剂采用热熔融法制备,条件苛刻。
综上所述,低碳炔烃和二烯烃的选择性加氢,目前主要采用贵金属催化剂,对于非贵金属催化剂的研发开展大量工作,但是距离工业化应用尚有很远的距离。为了解决这一问题,本发明提供一种Fe系加氢催化剂及其制备方法。
发明内容
本发明的目的是提供一种Fe系催化剂,用于碳二馏分中炔烃和二烯烃选择性加氢。采用本发明的催化剂,可以将裂解气氛中所含少量乙炔和丙炔(MA)、丙二烯(PD)进行选择性加氢,转化为乙烯、丙烯。也可以用于乙烯、丙烯精制反应,将乙烯、丙烯原料气中所含微量乙炔和丙炔(MA)、丙二烯(PD)完全去除,用于生产聚合级原料。
为了达到上述目的,本发明采用以下技术方案:以耐高温无机氧化物为载体的非贵金属催化剂,以催化剂质量100%计,催化剂含Fe 2~15%,优选含量为4~10%,X含量占0~2%,其中X选自K、La、Ce中的一种或者几种,X优选含量为0.2~1.5%;催化剂比表面为10~300m2/g优选30~170m2/g,孔容为0.2~0.65ml/g,优选0.30~0.63ml/g,其中Fe是通过浸渍方式载负于载体上,经300℃~700℃焙烧,用含氢气的气氛在250~500℃温度下还原制得,催化剂中的Fe元素主要以α-Fe2O3形式存在。
本发明的催化剂中Fe元素可以Fe、Fe2O3、Fe3O4、FeO等多种形态存在,但其中α-Fe2O3形态的Fe要比其它形态的含量要高,最好占Fe总质量的50%以上。
本发明的载体为耐高温无机氧化物,本发明的技术关键在于催化剂中含Fe,并且经过了焙烧与还原过程,对载体并无特别要求,如可以是氧化铝、氧化硅、氧化锆、氧化镁等中的一种或几种。但但最常见的也是最好的是氧化铝或氧化铝系载体,氧化铝系载体是指氧化铝与其他氧化物的复合载体,其中氧化铝占载体质量的50%以上,如可以是氧化铝与氧化硅、氧化锆、氧化镁等氧化物的复合物,最好是氧化铝-氧化锆复合载体,其中氧化铝含量在60%以上。氧化铝可以为θ、α、γ型或其多种晶型的混合物,最好是α-Al2O3或含α-Al2O3的混合晶型氧化铝。
本发明还提供了该催化剂的制备方法:
催化剂通过制备Fe前驱物水溶液、X前驱物水溶液,分别浸渍载体、分别陈化、干燥、焙烧或以其混合溶液浸渍载体后陈化、干燥、焙烧,最后还原获得。
本发明制备方法中优选的条件为:
浸渍温度30~60℃,浸渍时间10~60min,浸渍液pH值1.5~5.0,陈化温度30~60℃,陈化时间30~120min,焙烧温度400℃~500℃,焙烧时间180~300min。
本发明中焙烧即活化过程,最好为程序升温焙烧,焙烧温度程序设定为:
本发明中所述催化剂可以采用等体积浸渍、过量浸渍、表面喷浸、真空浸渍和多次浸渍法中的任意一种浸渍方式制备。
本发明推荐的催化剂制备方法的具体步骤如下:
(1)测量载体吸水率后称取载体。
(2)按负载量准确称取一定量的Fe前驱物(推荐可溶性硝酸盐、氯化物或硫酸盐),根据载体吸水率和浸渍方法,配制浸渍溶液,并按要求调节浸渍液pH值1.5~5.0,并将溶液加热到30~60℃备用。
(3)采用等体积浸渍或者喷浸法时,可将称取好的载体放入转鼓中,调节转鼓转速25~30转/min,使载体完全翻转起来,将配制好的30~60℃的浸渍液以一定速率倒入或喷洒到载体上,负载5~10min。
采用过量浸渍法时,将称取的载体置于容器中,然后加入配制的30~60℃的浸渍溶液,快速摇动容器,使吸附过程中放出的热量迅速释放,并使活性组分均匀负载到载体上,静置5~10min使表面活性组分与溶液中活性组分竞争吸附平衡。
采用真空浸渍法时,将称取好的载体置于旋流蒸发器中,抽真空,加入30~60℃的浸渍液浸渍5~10min,水浴加热至载体表面水分完全干燥。
(4)浸渍好的催化剂移入容器中,25~60℃下进行催化剂陈化30~120min。
催化剂X组分采用上述相同步骤进行负载,焙烧温度300~700℃,最好为400~500℃,两种组分也可以配制成混合溶液,按照上述步骤一次性浸渍至载体表面。
本发明还原是指催化剂使用前,需要用含氢气体还原,H2含量最好为10~50%,还原温度最好是250~500℃,还原时间240~360min,体积空速100~500h-1,还原压力0.1~0.8MPa;推荐的条件是使用N2+H2混合气在微正压条件下300~400℃进行还原,还原时间最好是240~360min,体积空速最好200~400h~1,还原压力最好为0.1~0.5MPa。
本发明中催化剂的活性组分主要是Fe,是非贵金属催化剂,甚至可以不含钴、镍、钼、钨,大大降低了成本,催化剂成本远低于贵金属Pd催化剂。
本发明催化剂中Fe元素可以以Fe、Fe2O3、Fe3O4、FeO中几种形态存在,本发明中推荐在含铁的活性组成中再加入K、La、Ce中的一种或者几种,有利于催化剂活化相的形成、分散,并且有利于活化相的稳定,提高催化剂选择性和抗结焦性能。
本发明中催化剂的活化温度与催化剂的活性组成、含量以及载体有关,经活化过程后形成了α-Fe2O3形态的Fe,并且较为稳定,活化温度不可过高;另一方面,其活化程度又决定了催化剂的还原条件,本发明中提供使用的催化剂中仍以α-Fe2O3形态的Fe为主要成分,过分还原反而会影响催化剂的效果,影响选择性,易结焦。
本发明催化剂具有以下有益效果:
(1)本发明催化剂成本远低于贵金属Pd催化剂,所用原材料无害易取得,并且制备方法简单,技术上易实现。
(2)本发明所述催化剂加氢活性温和,操作弹性好,适于工业化装置应用。
(3)本发明所述催化剂选择性好,烯烃增量高于贵金属催化剂。
(4)本发明所述催化剂“绿油”生成量远低于贵金属催化剂,适于催化剂长周期运行。
本发明的Fe系选择加氢催化剂最适用于乙烯气氛中所含乙炔和丙炔、丙二烯的选择性加氢脱除。
附图说明
附图1为应用本发明实施例3催化剂XRD谱图(扣除载体背景);
附图2为对比例2催化剂XRD谱图(扣除载体背景);
附图3为对比例5催化剂XRD谱图(扣除载体背景);
XRD测定条件:
德国布鲁克公司D8ADVANCE X衍射仪
管电压:40kV电流40mA
扫描:步长0.02°频率0.5s扫描范围4°~120°温度25℃
Cu Kα1波长,图中横坐标为衍射角2θ,纵坐标为衍射强度
图1中符号说明:
图2中符号说明:
●为α-Fe2O3,▲为Fe3O4,■为LaFeO3;
图3中符号说明:
▲为Fe3O4,▼为Ce,★为α-Fe;
图1中可以看出,催化剂中Fe主要以α-Fe2O3形式出现,相对含量7.6%;
图2中可以看出,催化剂中第二种组分La,主要与铁氧化物结合形成LaFeO3,助组分与活性组分烧结,破坏了活性组分分布和结构,催化剂活性下降;
图3中不含α-Fe2O3相,Fe主要以单质α-Fe形式出现,相对含量8.92%,第三组分以单质Ce形式出现。
具体实施方式
分析测试方法:
比表面:GB/T-5816
孔容:GB/T-5816
不同晶型Fe氧化物含量:XRD
催化剂中活性组分含量:原子吸收法
实施例中转化率和选择性按下面公式计算:
乙炔转化率(%)=100×△乙炔/入口乙炔含量
乙烯选择性(%)=100×△乙烯/△乙炔
实施例1
称取Φ4.5×4.5mm的三叶草型α-氧化铝载体100ml,置于1000ml烧杯中。取硝酸铁,加热溶解于60ml去离子水中,调节pH值2.5,浸渍液温度50℃,等体积浸渍于载体表面,迅速摇动载体浸渍6min,静置30min至吸附平衡,用保鲜膜完全密封烧杯口,在60℃水浴中陈化30min,然后在烘箱中按照程序:将催化剂移入蒸发皿,在马弗炉中采用程序升温法进行催化剂活化,活化程序: 称取硝酸镧,按照上述制备步骤进行浸渍。催化剂物性如表1所示。
评价方法:
在10ml微反装置上进行催化剂性能评价,催化剂在研钵中破碎,取10~20目筛分3ml,用20目玻璃珠稀释到5ml进行装填。
催化剂先用40%氢气+60%氮气进行还原,还原温度320℃,压力0.5MPa,还原时间4h。
反应条件:体积空速8000h-1,压力1.5MPa,反应温度80℃。
反应原料气采用标准气体,组成如下:
制备催化剂物性如表1所示,反应结果如表2所示。
实施例2
在50℃,将NaAlO2溶液和ZrCl4溶液搅拌混合,然后用硝酸溶液中和,搅拌10h,共沉淀生成均匀的Al-Zr颗粒。将生成物过滤,用去离子水洗涤其中的Na+和Cl-离子,然后加入适量质量浓度为15%的聚乙烯醇作为造孔剂,捏合成型。130℃干燥2h,650℃焙烧4h得到Zr-Al复合载体,载体中氧化铝与氧化锆质量比为4:1。
称取复合载体100ml,置于1000ml大烧杯中。取氯化铁和氯化钾,加热溶解于100ml去离子水中,调节pH值2.0,浸渍液温度80℃,过量浸渍到载体上,摇动烧杯浸渍10min,将多余浸渍液滤除,催化剂在60℃水浴中陈化50min,然后在烘箱中按照程序:将催化剂移入蒸发皿,在马弗炉中采用程序升温法进行催化剂活化,活化程序:催化剂物性如表1所示。
采用实施例1相同方法进行催化剂评价,用30%氢气进行还原,还原温度340℃,压力0.5MPa,还原时间4h。
反应条件:体积空速8000h-1,压力1.5MPa,反应温度80℃。
反应原料气采用标准气体,组成如下:
反应结果如表2所示。
实施例3
称取Φ1.5mm的球型α-氧化铝载体100ml。取硝酸铁溶解于40ml去离子水中,调节pH值3.0,浸渍液温度40℃,喷壶喷浸到载体上,在转鼓中负载10min使活性组分上载均匀,负载过程控制在6min完成,然后在烘箱中按照程序:将催化剂移入蒸发皿,在马弗炉中采用程序升温法进行催化剂活化,活化程序: 得到一浸催化剂。
催化剂物性如表1所示。
采用实施例1相同方法进行评价,催化剂用20%氢气进行还原,还原温度360℃,压力0.5MPa,还原时间4h。
反应条件:体积空速8000h-1,压力1.5MPa,反应温度80℃。
反应原料气采用标准气体,组成如下:
反应结果如表2所示。
实施例4
称取50ml的Φ2.0mm的球形氧化铝-氧化钛载体,置于旋转蒸发器中。取硝酸铁溶解于15ml去离子水中,调节pH值3.5备用。打开旋转蒸发器抽真空泵,至真空度0.1mmHg,然后从加料口缓慢加入配制好的浸渍液,5min加完,在60℃水浴加热下旋转蒸发至催化剂表面流动水分完全消失,完成负载,将负载好的催化剂移出旋转蒸发器,在烘箱中按照程序: 在马弗炉中按照: 得到一浸催化剂。
催化剂物性如表1所示。
采用实施例1相同方法进行评价,催化剂用15%氢气进行还原,还原温度380℃,压力0.5MPa,还原时间4h。
反应条件:体积空速8000h-1,压力1.5MPa,反应温度80℃。
反应原料气采用标准气体,组成如下:
制备催化剂物性如表1所示,反应结果如表2所示。
实施例5
称取100mlΦ4.0mm的氧化铝载体,采用实施例3相同方法制备催化剂。活化温度650℃。
催化剂物性如表1所示。
催化剂用25%氢气进行还原,温度700℃,压力0.5MPa,活化时间4h。
采用实施例1相同方法进行评价。
反应条件:体积空速8000h-1,压力1.5MPa,反应温度80℃。
反应原料气采用标准气体(乙烷平衡气),组成如下:
制备催化剂物性如表1所示,反应结果如表2所示。
实施例6
将市售拟薄水铝石、硅胶、氧氯化锆粉末和助挤剂按照氧化铝:氧化硅:氧化锆=8:1:3比例混合均匀,然后在挤条机上挤条成型,120℃干燥,在马弗炉中550℃焙烧3h,得到Zr-Si-Al复合氧化物载体。
称取50ml制备的Zr-Si-Al载体,采用实施例4相同方法制备催化剂。
催化剂物性如表1所示。
催化剂在管式炉中进行高温活化,活化气氛为45%氢气+55%氮气,温度450℃,压力0.5MPa,活化时间4h。制备催化剂物性如表1所示。
采用实施例1相同方法进行评价。
反应条件:体积空速8000h-1,压力1.5MPa,反应温度80℃。
反应原料气采用标准气体(乙烷为平衡气),组成如下:
反应结果如表2所示。
实施例7
取Φ4.0mm的氧化铝作载体,采用实施例1相同方法制备催化剂,在450℃进行活化。
催化剂使用前,用20%氢气进行还原,温度450℃,压力0.5MPa,活化时间4h。采用实施例1相同方法进行评价。
反应条件:体积空速8000h-1,压力2.5MPa,反应温度50℃。
反应原料气采用标准气体(乙烷平衡气),组成如下:
制备催化剂物性如表1所示,反应结果如表2所示。
对比例1
取Φ4.0mm氧化铝载体,比表面为4.5m2/g,孔容为0.32ml/g。采用等体积浸渍法,将硝酸银溶液等体积浸渍到载体上,陈化-干燥-焙烧,得到一浸催化剂,然后将氯化钯溶解,等体积浸渍,陈化-干燥-焙烧,得到最终催化剂(石化研究院PAH-01加氢催化剂)。催化剂Pd含量为0.050%,Ag含量为0.20%。
催化剂在100℃用氢气还原160min,压力0.5MPa,氢气体积空速100h-1。
评价原料气组成:
制备催化剂物性如表1所示,反应结果如表2所示。
对比例2
以Φ4.0mm氧化铝作载体,采用实施例1相同的方法制备催化剂,催化剂活化温度850℃。
催化剂用25%氢气进行还原,温度450℃,压力0.5MPa,时间4h。还原后催化剂的XRD衍射谱图如图2所示。
采用实施例1相同方法进行评价。
反应条件:体积空速8000h-1,压力1.5MPa,反应温度80℃。
反应原料气采用标准气体(乙烷平衡气),组成如下:
制备催化剂物性如表1所示,反应结果如表2所示。
对比例3
称取Φ4.0mm的氧化铝作载体,采用实施例1相同方法制备催化剂,在450℃进行活化。
催化剂用35%氢气进行还原,温度450℃,压力0.5MPa,活化时间4h。
采用实施例1相同方法进行评价。
反应条件:体积空速8000h-1,压力1.5MPa,反应温度80℃。
反应原料气采用标准气体(乙烷平衡气),组成如下:
制备催化剂物性如表1所示,反应结果如表2所示。
对比例4
取实施例1相同催化剂,在450℃活化后直接开车,不用氢气进行还原。
采用实施例1相同方法进行评价。
反应条件:体积空速8000h-1,压力1.5MPa,反应温度80℃。
反应原料气采用标准气体(乙烷平衡气),组成如下:
制备催化剂物性如表1所示,反应结果如表2所示。
对比例5
取实施例1相同催化剂,在450℃活化。
催化剂在管式炉中进行还原,气氛为30%氢气+55%氮气,温度850℃,压力0.5MPa,活化时间4h。还原后催化剂的XRD衍射谱图如图3所示。
制备催化剂物性如表1所示。
采用实施例1相同方法进行评价。
反应条件:体积空速8000h-1,压力1.5MPa,反应温度80℃。
反应原料气采用标准气体(乙烷为平衡气),组成如下:
反应结果如表2所示。
表1载体和催化剂物性
表2催化剂对C2-3裂解物料选择加氢结果
注:乙炔和乙烯聚和生成正丁烯,进一步聚和生成“绿油”,分析中通常用正丁烯生成量表征催化剂绿油”生成量。
Claims (15)
1.一种Fe系选择加氢催化剂,是非贵金属催化剂,其特征在于,以催化剂质量100%计,催化剂含Fe 2~15%,X 0.2~1.5%,其中X选自K、La、Ce中的一种或者几种;催化剂比表面为10~300m2/g,孔容为0.2~0.65mL/g,其中Fe是通过浸渍方式载负于载体上,经300℃~700℃焙烧,用含氢气的气氛在250~500℃温度下还原制得;催化剂中,Fe主要以α-Fe2O3形态存在。
2.根据权利要求1所述Fe系选择加氢催化剂,其特征在于:以催化剂质量100%计,催化剂含Fe4~10%;催化剂比表面为30~170m2/g,孔容为0.30~0.63mL/g。
3.根据权利要求1所述Fe系选择加氢催化剂,其特征在于:催化剂中,α-Fe2O3形态的Fe要占Fe总质量的50%以上。
4.根据权利要求1所述Fe系选择加氢催化剂,其特征在于:载体是氧化铝或氧化铝系载体,氧化铝系载体是指氧化铝与其他氧化物的复合载体,其中氧化铝占载体质量的50%以上;氧化铝为θ、α、γ型或其多种晶型的混合物。
5.根据权利要求4所述Fe系选择加氢催化剂,其特征在于:所述氧化铝系载体是氧化铝与氧化硅、氧化锆、氧化镁的复合物,其中氧化铝含量在60%以上。
6.根据权利要求5所述Fe系选择加氢催化剂,其特征在于:所述氧化铝系载体是氧化铝-氧化锆复合载体;氧化铝为α-Al2O3或含α-Al2O3的混合晶型氧化铝。
7.根据权利要求1所述Fe系选择加氢催化剂,其特征在于所述浸渍方式为等体积浸渍、过量浸渍、表面喷浸、真空浸渍或多次浸渍。
8.一种权利要求1-7任一所述Fe系选择加氢催化剂的制备方法,其特征在于:催化剂的制备过程包括:制备含Fe前驱物水溶液、X前驱物水溶液的浸渍液,分别浸渍载体、分别陈化、干燥、焙烧或以其混合溶液浸渍载体后陈化、干燥、焙烧,最后还原获得。
9.根据权利要求8所述的Fe系选择加氢催化剂的制备方法,其特征在于:浸渍温度30~60℃,浸渍时间10~60min,浸渍液pH值1.5~5.0,陈化温度30~60℃,陈化时间30~120min,焙烧温度300℃~700℃,焙烧时间180~300min。
10.根据权利要求9所述的Fe系选择加氢催化剂的制备方法,其特征在于:所述焙烧温度为400~500℃。
13.根据权利要求8所述的Fe系选择加氢催化剂的制备方法,其特征在于:催化剂还原是指催化剂使用前,焙烧后的催化剂用含氢气体还原,H2体积含量为10~50%,还原温度250~500℃,还原时间240~360min,体积空速100~500h-1,还原压力0.1~0.8MPa。
14.根据权利要求13所述的Fe系选择加氢催化剂的制备方法,其特征在于:所述催化剂还原的条件为:用N2+H2混合气进行,在300~400℃下,体积空速200~400h-1,还原压力为0.1~0.5MPa。
15.一种权利要求1所述Fe系选择加氢催化剂的应用,其特征在于:Fe系选择加氢催化剂用于乙烯气氛中所含乙炔、丙炔、丙二烯的选择性加氢脱除。
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