CN102172531A - 用于氢化芳族化合物的铜改性的镍催化剂 - Google Patents

用于氢化芳族化合物的铜改性的镍催化剂 Download PDF

Info

Publication number
CN102172531A
CN102172531A CN2011100599847A CN201110059984A CN102172531A CN 102172531 A CN102172531 A CN 102172531A CN 2011100599847 A CN2011100599847 A CN 2011100599847A CN 201110059984 A CN201110059984 A CN 201110059984A CN 102172531 A CN102172531 A CN 102172531A
Authority
CN
China
Prior art keywords
catalyst
hydrogenation
benzene
cyclohexane
reactor
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
Application number
CN2011100599847A
Other languages
English (en)
Inventor
J·荣·刘
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Catalytic Distillation Technologies
Original Assignee
Catalytic Distillation Technologies
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Catalytic Distillation Technologies filed Critical Catalytic Distillation Technologies
Publication of CN102172531A publication Critical patent/CN102172531A/zh
Pending legal-status Critical Current

Links

Classifications

    • 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
    • B01J23/889—Manganese, technetium or rhenium
    • B01J23/8896—Rhenium
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C209/00—Preparation of compounds containing amino groups bound to a carbon skeleton
    • C07C209/68—Preparation of compounds containing amino groups bound to a carbon skeleton from amines, by reactions not involving amino groups, e.g. reduction of unsaturated amines, aromatisation, or substitution of the carbon skeleton
    • C07C209/70—Preparation of compounds containing amino groups bound to a carbon skeleton from amines, by reactions not involving amino groups, e.g. reduction of unsaturated amines, aromatisation, or substitution of the carbon skeleton by reduction of unsaturated amines
    • C07C209/72—Preparation of compounds containing amino groups bound to a carbon skeleton from amines, by reactions not involving amino groups, e.g. reduction of unsaturated amines, aromatisation, or substitution of the carbon skeleton by reduction of unsaturated amines by reduction of six-membered aromatic rings
    • 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
    • B01J23/74—Iron group metals
    • B01J23/755—Nickel
    • 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
    • B01J23/80—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 zinc, cadmium or mercury
    • 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
    • B01J23/883—Molybdenum and nickel
    • 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
    • B01J23/89—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals
    • B01J23/892—Nickel and noble metals
    • 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
    • B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C209/00—Preparation of compounds containing amino groups bound to a carbon skeleton
    • C07C209/02—Preparation of compounds containing amino groups bound to a carbon skeleton by substitution of hydrogen atoms by amino groups
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
    • C07C5/02—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation
    • C07C5/10—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation of aromatic six-membered rings
    • 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
    • B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
    • B01J35/61—Surface area
    • B01J35/613—10-100 m2/g
    • 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
    • B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
    • B01J35/61—Surface area
    • B01J35/615—100-500 m2/g
    • 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
    • B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
    • B01J35/63—Pore volume
    • B01J35/633—Pore volume less than 0.5 ml/g
    • 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
    • B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
    • B01J35/63—Pore volume
    • B01J35/635—0.5-1.0 ml/g
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
    • C07C2523/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of the iron group metals or copper
    • C07C2523/74—Iron group metals
    • C07C2523/75—Cobalt
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
    • C07C2523/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of the iron group metals or copper
    • C07C2523/74—Iron group metals
    • C07C2523/755—Nickel
    • 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
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
  • Catalysts (AREA)

Abstract

本发明提供一种用于氢化芳族化合物以生产氢化环状化合物的铜改性的镍催化剂，所述催化剂包括沉积在过渡型氧化铝载体上的4-14wt％Ni和0.2-0.4wt％的Cu，所述过渡型氧化铝载体的BET表面积为40-180m2/g，孔体积为0.3-0.8cc/g，其中所述催化剂包含选自Ag和Ru中的一种或多种改性剂。本发明催化剂的性能优于常规的镍催化剂。

Description

用于氢化芳族化合物的铜改性的镍催化剂
本发明专利申请是基于2007年2月1日提交的发明名称为“芳族化合物的氢化”的中国专利申请200710006317.6号的分案申请。
技术领域
本发明涉及一种氢化芳族化合物的方法，比如将苯氢化为环己烷，和所用的由最高达0.9wt％的Cu改性的负载镍催化剂。
背景技术
环己烷是制造尼龙产品的主要前体，正因如此，仍保持旺盛需求。环己烷最初通过直接分馏适当的原油炼油厂物流获得。现在，环己烷的主要部分从直接氢化苯获得。通常，反应在蒸气或混合相使用固定床反应进行。所述反应器温度控制在350-500℉之间。更高的温度可能导致对苯转化率的热力学限制，导致热裂化和副产物增加。通常，在加氢反应器流出物物流中的副产物量随着氢化温度或苯的转化率或随两者而增加。
Peterson在US专利2,373,501中公开了将苯氢化为环己烷的液相方法，其中催化剂床的顶部与出口处之间保持温差，在所述催化床的顶部加入苯，在所述出口处引出基本纯的环己烷。所述温差源自于随苯浓度减少而越来越少的苯发生转化，引起反应释放的热的变化。特别地，催化剂床的顶部比较低的催化剂床处于较高的温度。以与苯/环己烷流逆流的方式提供氢。在所述反应器之内布置温控线圈，如果反应放出的热不够则保持所述温差，或如果释放太多的热则冷却所述床。Peterson认识到虽然他的大多数反应在液相发生，但一部分苯和环己烷将被蒸发了，尤其是接近所述反应器顶部的苯和环己烷，在反应器的顶部苯浓度最高，转化率最高。提供回流冷凝器以冷凝可冷凝的物质，并将它们返回到所述反应器中。因此，通过冷凝整个反应中蒸发的反应物除去相当大部分的反应热。Peterson保持液位高于催化剂床的最顶端，但是留出用于蒸气逸出到所述冷凝器的空间，在冷凝器处除去反应热。
Larkin等人在US专利5,189,233中公开了另一种将苯氢化为环己烷的液相方法。然而，Larkin等人利用高压(2500磅/平方英寸)保持反应物处于液态。另外，Larkin等人公开了使用随苯浓度降低活性逐渐更高的催化剂控制温度和不需要的副反应。
Hui等人在US专利4,731,496中公开了用特定的催化剂将苯氢化为环己烷的气相方法。在其中报导的所述催化剂是负载在二氧化钛和二氧化锆混合物上的镍。
US专利6,750,374公开了利用氢氢化苯的方法，所述的氢含高达约15摩尔％的杂质，比如一氧化碳和轻质烃，使用包括约15-35wt％Ni和约1-15wt％Cu的氧化铝负载催化剂。所述催化剂可以包含另外的元素比如Mo，Zn，Co，Fe。
发明内容
本发明涉及一种氢化芳族化合物的方法和用于所述方法的催化剂，所述的芳族化合物如苯，苯胺，萘，酚和苯聚羧酸酯，该方法通过在催化剂存在下氢化所述芳族化合物而实现，所述催化剂包括沉积在过渡型氧化铝载体上的4-14wt％的Ni，优选9-10wt％的Ni和最高达约0.9wt％的Cu，优选约0.2-0.4wt％的Cu，所述过渡型氧化铝载体的BET表面积为约40-180m2/g和孔体积为约0.3-约0.8cc/g。所述芳族化合物的氢化有利地在高沸点溶剂的存在下进行。优选溶剂的沸点比待氢化的芳化合物和氢化的环状化合物高至少10℉。使用高沸点溶剂的优点是得到较高的环己烷生产量，并使催化反应区温度保持在希望的范围。不管所述镍催化剂是否用铜进行改性，所述高沸点溶剂可改进反应体系的生产能力。
在环己烷的生产中，反应物流中的苯含量为1-60wt％，优选3-40wt％。所述氢气流可以是纯氢或可以包含最高达5摩尔％的包括一氧化碳的杂质。所述反应流中的其余组分可以是环己烷，高沸点溶剂或环己烷和高沸点溶剂的混合物。如果使用高沸点溶剂，所述溶剂可以占反应物流的10-90wt％，优选20-80wt％。可以从所述流出物再循环物流中回收所述高沸点溶剂，并再循环到加氢反应器中。在再循环溶剂物流中环己烷的含量可以为0.0-80wt％，优选0.5-30wt％。
本发明同样涉及用于氢化芳族化合物以生产氢化环状化合物的铜改性的镍催化剂，所述催化剂包括沉积在过渡型氧化铝载体上的4-14wt％的Ni和约0.2-0.4wt％的Cu，所述过渡型氧化铝载体的BET表面积为约40-180m2/g，和孔体积为约0.3-约0.8cc/g。
具体实施方式
本发明涉及在改进的负载于多孔载体上的铜改性镍基催化剂的存在下，芳族化合物比如苯，苯胺，萘和酚的催化氢化方法。苯的氢化得到环己烷。但是，来自催化反应器的氢化产品流包含其它不希望的副产物，比如戊烷，环戊烷，甲基环戊烷，正己烷和甲基环己烷。所述的产品物流通常包含痕量的苯，最高达约200重量ppm。对于生产高纯度的环己烷，非常希望苯小于10ppm。通常，在来自加氢反应器流出物物流中的副产物量随着氢化温度或苯的转化率或随两者而增加。尤其是，所述副产物的量在高于约340℉的氢化温度下迅速增加。苯胺的氢化得到环己胺。但是，不希望的副反应是脱氨基作用，形成二苯胺和三苯胺和不同的重质产品。本发明的优点是副产物减少，因此简单蒸馏氢化产品物流即可生产高纯度的环己烷产品。优选，所述环己烷产品包含按重量至多约50ppm，优选至多30ppm的包括未转化的苯的杂质，不包括原料苯带来的杂质。所述加氢反应器流出物包含少量的环己烯。因为通过再循环反应器流出物或使用小的分离反应器，环己烯能容易地氢化为环己烷，而不会不产生大量的副产物，所以它不被认为是不希望的副产物。如果苯氢化在重质溶剂比如十氢化萘和癸烷存在下进行，本发明可显著改进环己烷的生产能力以及将来自催化反应区的产物环己烷物流中的总杂质减少到小于10ppm。使用重质溶剂的另外的优点在于氢的循环基本更少。
所述氢化反应可以在任何的物理设备中比如催化蒸馏塔，固定床反应器，沸点反应器，搅拌釜反应器，滴流床反应器或这些反应器的任意组合中进行。因为所述苯氢化反应是放热反应，所以对于常规的固定床操作氢化反应优选通过再循环反应器流出物物流以稀释新鲜的苯原料而进行，这样冲淡反应热。虽然对于催化蒸馏反应器再循环反应器流出物不是必要的，但可以选择如此进行。
本发明催化剂优选包括Ni和Cu，并任选包括一种或多种选自Ag，Ru，Re，Zn，Mo和Pd的元素，所述的元素沉积在包括过渡氧化铝的载体上，所述过渡氧化铝如γ，κ，δ，θ和α的结晶氧化铝，或包括其中选择的两种或三种的混合物。优选所述催化剂的镍含量为约9-10wt％，优选的铜含量为约0.2-0.4wt％。用于本发明的催化剂通过将镍和铜沉积在多孔载体上而制备。铜用于改善催化剂的活性和选择性。所述催化剂可以包含一种或多种选自Ag，Ru，Re，Zn，Mo和Pd的元素作为第二任选的改性剂。活性金属组分的沉积可以通过任何一种技术比如初始浸渍，喷涂浸渍进行。优选载体的平均尺寸为约0.5毫米-约3毫米，优选约1毫米-约2.5毫米。
所述过渡型氧化铝通过在大约850-约1200℃焙烧获得，并优选在850-1200℃焙烧之后具有以下物理性质：BET表面积为约40-约180m2/g，优选为50-120m2/g，孔体积为约0.3-约0.8cc/g。所述过渡型氧化铝是δ，θ，κ结晶氧化铝，或来自γ，κ，δ，θ和α的两种或三种组成的混合物。
在本发明中优选的氧化铝的物理形状可以是任何形状比如球状，挤出物，小球状和颗粒，优选直径小于约1/4英寸，优选1/8英寸，和小于约1/2英寸长，并优选小于1/4英寸长的挤出物或小球状。
通过一个或多个浸渍步骤可以将镍沉积在载体上。通过将镍化合物或有机镍化合物溶解在有机溶剂或水中制备镍化合物的溶液。所述镍化合物的例子有镍盐，比如硝酸镍或有机金属镍化合物，比如乙酸镍，甲酸镍，乙酰基丙酮酸镍和醇镍。在200℃-600℃，优选250℃-500℃的温度范围下干燥和焙烧浸渍的产品。
当所述苯的氢化是在沸点模式下操作的固定床反应器中或在催化蒸馏反应器中进行时，利用氢化反应的热来蒸发产品环己烷。蒸发的结果是氢化反应区的内部冷却。来自催化蒸馏反应器的塔顶蒸气物流包括环己烷和氢，所述的催化蒸馏反应器在存在高沸点溶剂或不存在高沸点溶剂的条件下操作。
对照实施例1
测试工业用的28wt％Ni催化剂(1.2毫米直径的三叶挤出物)氢化苯。该催化剂的氧化铝载体的晶形是γ-氧化铝。该催化剂的物理性质是BET为113m2/g，总氮孔体积为0.43cc/g，平均孔径为15纳米。将50克所述催化剂装填在垂直安装的上流式不锈钢固定床反应器(1英寸直径×20英寸长)中。在催化剂区的每一端安置两个热电偶以控制反应器温度。所述催化剂由制造商提供，为活化和钝化形式，推荐在482℉氢气流中再活化。所述催化剂在250℉下在300cc/min的气流中再活化1.5小时，所述气流为氮气中33体积％的氢气，然后在575℉下在350cc/min的纯氢气流中再活化5小时。苯的氢化在不同的条件下进行。所述结果列于表1中。
表1
Figure BSA00000449588700061
实施例2
将圆球形的γ-氧化铝(直径1.68毫米)载体在1100℃焙烧3小时。焙烧之前氧化铝小球的BET表面积为145m2/g，总氮体积为0.925cc/g，平均孔径为21.6纳米。在焙烧之后，氧化铝小球的直径变为1.45毫米，BET为56m2/g，总氮孔体积为0.701cc/g，平均孔径为36.2纳米。其X-光衍射表明大部分为θ-氧化铝，有微量的δ-氧化铝。
通过在25.95克水中溶解86.5克的Ni(NO3)2·2.5H2O制备硝酸镍和硝酸铜的混合溶液。将300克的焙烧氧化铝放置在旋转浸渍设备中。该混合溶液通过使用液体喷雾器在约15分钟内在旋转浸渍设备内部喷雾到旋转的氧化铝小球上。通过吹入约200℃的热空气干燥所述旋转浸渍设备中的内容物。所述干燥产品在350℃焙烧2小时。
通过在19.5克水中溶解65克的Ni(NO3)2·6H2O和1.8克的Cu(NO3)2·2.5H2O制备第二混合溶液。以类似第一浸渍的方式在第一浸渍产品上实施第二浸渍。所述干燥的浸渍产品在380℃焙烧2小时。
基于使用的材料量，成品催化剂将包含9.22wt％的Ni和0.35wt％的Cu。在显微镜下观查所述催化剂小球表明，所述活性金属组分沉积在小球的外层。平均层厚度大约0.33毫米。该催化剂的物理性质是60m2/g，总氮孔体积为0.56cc/g和平均孔径为39纳米。将50克的该催化剂装填在与对照实施例1中使用的相同反应器中。所述催化剂在250℉在300cc/min的气流中活化1.5小时，所述气流为氮气中33体积％的氢气，然后各自在670℉和770℉的温度下通过350cc/min的纯氢气活化3小时。所述苯的氢化在不同的条件下进行。结果列于表2中。如表2所示，来自反应器的氢化反应产物物流不含任何可检测出量的副产物。该催化剂的性能优于常规的镍催化剂。
表2
Figure BSA00000449588700071
Figure BSA00000449588700081
实施例3
根据US公开2005-0033099-A制备镍催化剂。γ-氧化铝(直径1.3毫米的三叶挤出物)在大约1000℃在空气中焙烧3小时。所述γ-氧化铝的BET为252m2/g，总氮孔体积为0.571cc/g和平均孔径为8.85纳米。通过将183.6gNi(NO3)2·6H2O溶解在295克水中制备硝酸镍溶液。将300g所述煅烧的氧化铝载体放置在旋转浸渍设备中，然后将硝酸镍溶液倒在旋转浸渍设备中的翻滚的氧化铝挤出物上。在15分钟冷轧之后，旋转浸渍设备中的内容物在大约200℃通过将热空气鼓入旋转式干燥器中进行干燥。所述干燥产品在380℃下焙烧小时。基于用于制备该催化剂的硝酸镍的量，成品催化剂在氧化铝载体上将具有11wt％的Ni。所述成品催化剂物理性质的测定表明BET表面积为133m2/g，总氮孔体积为0.622cc/g和平均孔径为18.6纳米。
将50克该催化剂装填在与对照实施例1中使用的相同反应器中。所述催化剂以与实施例2相同的方式活化。苯的氢化在不同的条件下进行。结果列于表3中。比较表3中该催化剂的性能数据和表1中的对照实施例1的性能数据，表明该催化剂的性能优于常规的镍催化剂，尽管它没有在实施例2中的催化剂的性能数据一样好。
表3
Figure BSA00000449588700082
实施例4
该实施例说明在没有重质溶剂的情况下，利用循环反应器流出物进行苯的氢化。但是，被送到反应器的原料包括新鲜的苯原料和反应器流出物物流--环己烷。该试验说明氢化送去氢化的混合原料流，其中所述混合的原料表示通过混合1重量份的新鲜的苯和3重量份的反应器流出物循环蒸汽获得的物流。
将与实施例2相同的催化剂(50克)装填在与对照实施例1使用的相同反应器中。以与实施例2相同的方式活化催化剂。制备苯和环己烷的原料混合物。所述原料的组成是0.11wt％的轻物质，25.41wt％的苯和74.48wt％的环己烷。所述苯的氢化在不同的条件下进行。所述原料和产品流中的杂质用痕量分析方法分析。结果列于表4中。产品流中的杂质大部分来源于原料中的杂质。根据本发明在苯氢化期间产生的不同的杂质所有结合的总量小于10ppm。可以强制使苯的转化率达到这样高的程度，使得反应器流出物物流中的苯含量可以被减少到小于35wtppm。该实施例表明可以得到极其高的苯转化率(＞99.99％)，同时环己烷选择性相当于约99.999摩尔％。在表4中的右边两栏的两种条件下环己烷的生产能力为每kg催化剂为29.2和31.8m/fur。这证明与现有技术相比实施例1具有优异的催化剂性能。
表4
Figure BSA00000449588700101
实施例5
该实施例说明在十氢化萘作为高沸点溶剂存在下苯的氢化，其中苯转化为环己烷的转化率接近100％。
将实施例2制备的50克催化剂装填在与对照实施例1中使用的相同反应器中。所述催化剂以与实施例2相同的方式活化。所述原料是0.44wt％的轻物质，25.26wt％的苯和74.30wt％十氢化萘的混合物。在所述原料中沸点温度接近环己烷总的结合杂质平均大约为14.8ppm。苯的氢化在不同的条件下进行。用通常的gc分析法和痕量gc分析法分析所述原料和产品物流中的杂质。结果列于表5中。在不同的条件下产品中的杂质大部分来源于原料中的杂质。根据本发明，在苯氢化期间产生的所有不同杂质结合的总量基于100％环己烷小于4wtppm。在给定的苯的进料速度下，通过调节加入加氢反应器中氢的流速，在产品物流中痕量的苯可以被减少到在产品环己烷中小于2ppm。
在任何产品物流中均意想不到地没有发现痕量的环己烯。环己烷的生产率至少高于实施例4中在没有高沸点溶剂的情况下实施氢化的生产率的40％。
表5
Figure BSA00000449588700121
实施例6
该实施例说明在癸烷作为高沸点溶剂存在下苯的氢化。苯的转化率高到以致产品物流中苯含量接近于检测不到的水平。
将在实施例2中制备的50克催化剂装填在与对照实施例1使用的相同反应器中。所述催化剂以与实施例2相同的方式活化。所述原料是0.10wt％轻物质，30.26wt％的苯和69.64wt％的癸烷的混合物。在所述原料中沸点温度接近环己烷总的结合的杂质(不包括苯)平均大约为5.77ppm。苯的氢化在不同的条件下进行。所述原料和产品物流中的杂质用通常的gc分析法和痕量gc分析法进行分析。所述结果列于表6中。在不同的条件下产品中的杂质大部分来源于原料中的杂质。根据本发明，在苯氢化期间产生的所有不同的杂质结合的总量基于100％环己烷大约为11ppm。环己烷的生产率与在实施例4中在没有高沸点溶剂存在下实施氢化情况的生产率相当或更好。
表6
Figure BSA00000449588700131

Claims (3)

1.一种用于氢化芳族化合物以生产氢化环状化合物的铜改性的镍催化剂，所述催化剂包括沉积在过渡型氧化铝载体上的4-14wt％Ni和0.2-0.4wt％的Cu，所述过渡型氧化铝载体的BET表面积为40-180m2/g，孔体积为0.3-0.8cc/g，
其中所述催化剂包含选自Ag和Ru中的一种或多种改性剂。
2.根据权利要求1的催化剂，其中所述催化剂的Ni含量为9～10wt％。
3.根据权利要求1的催化剂，其中所述催化剂还包含选自Re、Zn、Mo和Pd中的一种或多种改性剂。
CN2011100599847A 2006-03-27 2007-02-01 用于氢化芳族化合物的铜改性的镍催化剂 Pending CN102172531A (zh)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US11/389,955 US7348463B2 (en) 2006-03-27 2006-03-27 Hydrogenation of aromatic compounds
US11/389,955 2006-03-27

Related Parent Applications (1)

Application Number Title Priority Date Filing Date
CN2007100063176A Division CN101045669B (zh) 2006-03-27 2007-02-01 芳族化合物的氢化

Publications (1)

Publication Number Publication Date
CN102172531A true CN102172531A (zh) 2011-09-07

Family

ID=38534396

Family Applications (2)

Application Number Title Priority Date Filing Date
CN2007100063176A Expired - Fee Related CN101045669B (zh) 2006-03-27 2007-02-01 芳族化合物的氢化
CN2011100599847A Pending CN102172531A (zh) 2006-03-27 2007-02-01 用于氢化芳族化合物的铜改性的镍催化剂

Family Applications Before (1)

Application Number Title Priority Date Filing Date
CN2007100063176A Expired - Fee Related CN101045669B (zh) 2006-03-27 2007-02-01 芳族化合物的氢化

Country Status (8)

Country Link
US (2) US7348463B2 (zh)
EP (1) EP1999101A4 (zh)
JP (1) JP2009531426A (zh)
KR (1) KR20080108140A (zh)
CN (2) CN101045669B (zh)
RU (1) RU2391326C1 (zh)
TW (1) TW200736209A (zh)
WO (1) WO2007126421A1 (zh)

Families Citing this family (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8518851B2 (en) * 2007-10-19 2013-08-27 Shell Oil Company Catalyst for the hydrogenation of unsaturated hydrocarbons and process for its preparation
US8119558B2 (en) * 2008-03-14 2012-02-21 Süd-Chemie Inc. Ultra high temperature shift catalyst with low methanation
DE102008026094A1 (de) * 2008-05-30 2009-12-03 Süd-Chemie AG Verfahren zur Herstellung nanokristalliner Nickeloxide
DE102008058971A1 (de) * 2008-11-25 2010-07-15 Süd-Chemie AG Schalenkatalysator, Verfahren zu seiner Herstellung sowie Verwendung
CN103030487B (zh) * 2011-09-29 2016-02-10 中国石油化工股份有限公司 芳烃加氢饱和的方法
CN102516087B (zh) * 2011-10-25 2013-10-30 江苏诺盟化工有限公司 一种高纯度二环己胺的制备方法
CN102925935B (zh) * 2012-11-13 2015-05-20 上海应用技术学院 一种镍-铜-三氧化二铝催化分离复合膜及其制备方法和应用
CN103638949B (zh) * 2013-12-09 2015-11-11 江苏大学 一种纳米镍/银/铜复合催化剂的制备及其应用
JP6306370B2 (ja) * 2014-02-25 2018-04-04 千代田化工建設株式会社 芳香族化合物の水素化システムおよび水素化方法
JP6456204B2 (ja) 2015-03-24 2019-01-23 千代田化工建設株式会社 芳香族炭化水素の水素化触媒及びそれを用いた水素化処理方法
CN105126867B (zh) * 2015-08-03 2018-03-16 浙江大学 一种碳负载Pt‑Ru‑Ni催化剂及其制备方法和应用
JP2019531873A (ja) 2016-08-18 2019-11-07 ザ ユニバーシティ オブ シカゴＴｈｅ Ｕｎｉｖｅｒｓｉｔｙ Ｏｆ Ｃｈｉｃａｇｏ 高度に効率的な有機変換のための金属酸化物に支持された地球に豊富な金属の触媒
KR102327050B1 (ko) 2017-12-29 2021-11-15 한화솔루션 주식회사 선택적 수소화 방법
FR3091659B1 (fr) * 2019-01-15 2023-04-14 Ifp Energies Now Procédé de préparation d’un catalyseur d’hydrogénation des aromatiques comprenant une étape de formation d’un alliage de NiCu en pré-imprégnation
US11376567B2 (en) * 2019-12-05 2022-07-05 GM Global Technology Operations LLC Methods for preparing catalytic systems
CN114522717B (zh) * 2022-03-09 2023-09-05 北京海顺德钛催化剂有限公司 一种加氢脱苯催化剂的制备方法及催化剂和应用

Family Cites Families (50)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2373501A (en) * 1942-04-18 1945-04-10 Du Pont Preparation of cyclohexane
US3108888A (en) * 1960-08-04 1963-10-29 Du Pont Colloidal, anisodiametric transition aluminas and processes for making them
US3346340A (en) * 1966-08-11 1967-10-10 Universal Oil Prod Co Production of bromine by oxidation of hydrogen bromide
DE1667210B2 (de) * 1966-12-20 1976-05-06 Nippon Oil Co., Ltd., Tokio Verfahren zur herstellung eines fuer eine selektive hydrierung von acetylenkohlenwasserstoffen geeigneten kupfer-nickel-katalysators
FR1549207A (zh) * 1967-03-24 1968-12-13
JPS4931433B1 (zh) * 1970-02-25 1974-08-21
US3706858A (en) * 1971-04-14 1972-12-19 Mc Graw Edison Co Supervisory control system for selectively connecting recorders and transcribing stations
FR2240905B1 (zh) * 1973-08-16 1980-01-04 Inst Francais Du Petrole
US4034062A (en) * 1975-03-20 1977-07-05 Borden, Inc. Removal of oxygen from gas stream with copper catalyst
US4073750A (en) * 1976-05-20 1978-02-14 Exxon Research & Engineering Co. Method for preparing a highly dispersed supported nickel catalyst
JPS5414939A (en) * 1977-07-07 1979-02-03 Agency Of Ind Science & Technol Hydrogenation of aromatic compound
US4160745A (en) * 1977-12-01 1979-07-10 Exxon Research & Engineering Co. Method of preparing highly active nickel catalysts and catalysts prepared by said method
US4172810A (en) * 1978-05-08 1979-10-30 Exxon Research & Engineering Co. Catalysts for the conversion of relatively low molecular weight hydrocarbons to high molecular weight hydrocarbons and the regeneration of the catalysts
US4471144A (en) * 1982-12-13 1984-09-11 Uop Inc. Theta-alumina as a hydrothermally stable support in hydrogenation
FR2546078B1 (fr) * 1983-05-19 1987-05-07 Pro Catalyse Procede de fabrication de catalyseurs pour le traitement des gaz d'echappement des moteurs a combustion interne
DD217996A1 (de) * 1983-08-04 1985-01-30 Leuna Werke Veb Verfahren zur herstellung eines katalysators fuer die glucosehydrierung
US4731496A (en) * 1986-07-25 1988-03-15 Chinese Petroleum Corporation Process for the hydrogenation of benzene to cyclohexane
FR2619391B1 (fr) * 1987-08-14 1990-01-12 Eurecat Europ Retrait Catalys Procede de reduction d'un catalyseur de raffinage avant sa mise en oeuvre
US4795733A (en) * 1987-11-27 1989-01-03 Gaf Corporation Hydrogenation catalyst and process for its preparation
US5189233A (en) * 1991-08-23 1993-02-23 Texaco Chemical Company Process for the production of cyclohexane by liquid phase hydrogenation of benzene
JP3023809B2 (ja) * 1991-12-24 2000-03-21 雪印乳業株式会社 環状有機化合物の水素化還元方法
US5352835A (en) * 1993-02-08 1994-10-04 Texaco Chemical Company Supported catalysts for amination
DE69521289T2 (de) * 1993-12-22 2002-05-02 Union Carbide Chem Plastic Reduktive Aminierung zur selektiven Herstellung von Aminoethylethanolamin
US5773670A (en) 1995-03-06 1998-06-30 Gildert; Gary R. Hydrogenation of unsaturated cyclic compounds
US6022823A (en) * 1995-11-07 2000-02-08 Millennium Petrochemicals, Inc. Process for the production of supported palladium-gold catalysts
US5856602A (en) 1996-09-09 1999-01-05 Catalytic Distillation Technologies Selective hydrogenation of aromatics contained in hydrocarbon streams
DE19734974A1 (de) * 1997-08-13 1999-02-25 Hoechst Ag Verfahren zur Herstellung von porös geträgerten Metall-Nanopartikel-haltigen Katalysatoren, insbesondere für die Gasphasenoxidation von Ethylen und Essigsäure zu Vinylacetat
US6218326B1 (en) * 1998-07-29 2001-04-17 University Of Iowa Research Foundation Supported molten-metal catalysts
DE19932060A1 (de) * 1999-07-12 2001-01-18 Basf Ag Verfahren zur Herstellung von C¶5¶-/C¶6¶-Olefinen
US6750374B2 (en) 1999-08-10 2004-06-15 Huntsman Petrochemical Corporation Manufacture of cyclohexane from benzene and a hydrogen source containing impurities
US6607678B2 (en) * 1999-08-17 2003-08-19 Battelle Memorial Institute Catalyst and method of steam reforming
US6187980B1 (en) 1999-09-29 2001-02-13 Catalytic Distillation Technologies Hydrogenation of benzene to cyclohexane
US6576588B2 (en) * 2000-04-07 2003-06-10 Catalytic Distillation Technologies Process for selective hydrogenation of alkynes and catalyst therefor
CN1179788C (zh) * 2000-09-29 2004-12-15 中国石油化工股份有限公司 不饱和烃选择加氢催化剂、其制备方法及其应用
AU2002341704A1 (en) 2001-10-15 2003-04-28 Catalytic Distillation Technologies Hydrogenation catalyst and hydrogenation process
US6680419B2 (en) * 2001-11-30 2004-01-20 Bp Corporation North America Inc. Process enhancing adsorbent capacity for acetylenic compounds
US20030105376A1 (en) * 2001-11-30 2003-06-05 Foral Michael J. Purification of polyolefin feedstocks using multiple adsorbents
US6429338B1 (en) 2002-01-17 2002-08-06 Air Products And Chemicals, Inc. Hydrogenation of single ring aromatic diamines
US6936568B2 (en) * 2002-06-12 2005-08-30 Sud-Chemie Inc. Selective hydrogenation catalyst
US20040030207A1 (en) * 2002-08-08 2004-02-12 Catalytic Distillation Technologies Selective hydrogenation of acetylenes
US6855853B2 (en) 2002-09-18 2005-02-15 Catalytic Distillation Technologies Process for the production of low benzene gasoline
RU2005115063A (ru) * 2002-10-16 2005-10-10 КонокоФиллипс Кампэни (US) Способ изготовления носителя для катализатора из стабилизированного переходного оксида алюминия (варианты), способ изготовления катализатора фишера-тропша и способ синтеза парафиновых углеводородов из синтез-газа
US7022645B2 (en) 2003-08-04 2006-04-04 Catalytic Distillation Technologies Ni hydrogenation catalysts, manufacture and use
US7919431B2 (en) * 2003-09-03 2011-04-05 Synfuels International, Inc. Catalyst formulation for hydrogenation
US20050113614A1 (en) * 2003-11-24 2005-05-26 Lowe David M. Catalyst and process for selective hydrogenation
US7199273B2 (en) * 2003-11-24 2007-04-03 Exxonmobil Chemical Patents, Inc. Selective hydrogenation of alkynes and/or diolefins
US7408089B2 (en) * 2004-03-19 2008-08-05 Catalytic Distillation Technologies Ni catalyst, process for making catalysts and selective hydrogenation process
DE102005019103B4 (de) * 2004-04-26 2023-09-21 Sasol Technology (Proprietary) Ltd. Verfahren zur Herstellung eines auf Cobalt basierenden Katalysators für die Fischer-Tropsch-Synthese und Verfahren zur Herstellung eines Fischer-Tropsch-Kohlenwasserstoffproduktes
US20060166816A1 (en) * 2004-06-23 2006-07-27 Catalytic Solutions, Inc. Catalysts and processes for selective hydrogenation of acetylene and dienes in light olefin feedstreams
US20060084830A1 (en) * 2004-10-20 2006-04-20 Catalytic Distillation Technologies Selective hydrogenation process and catalyst

Also Published As

Publication number Publication date
RU2008142366A (ru) 2010-05-10
EP1999101A1 (en) 2008-12-10
TW200736209A (en) 2007-10-01
JP2009531426A (ja) 2009-09-03
EP1999101A4 (en) 2009-08-19
CN101045669A (zh) 2007-10-03
US20070225531A1 (en) 2007-09-27
US7348463B2 (en) 2008-03-25
KR20080108140A (ko) 2008-12-11
RU2391326C1 (ru) 2010-06-10
WO2007126421A1 (en) 2007-11-08
CN101045669B (zh) 2011-07-13
US20080139383A1 (en) 2008-06-12

Similar Documents

Publication Publication Date Title
CN101045669B (zh) 芳族化合物的氢化
US7737079B2 (en) Ni catalyst, process for making catalysts and selective hydrogenation process
US7468342B2 (en) Catalysts and process for producing aromatic amines
CN1256309C (zh) 由烷烃制备烯烃、不饱和羧酸和不饱和腈的改进方法
PL157247B1 (en) Method of obtaining alcohol and catalyst forhadrogenation of aldehydes
US5942645A (en) Hydrogenation of aromatic compounds in which at least one hydroxyl group is bonded to an aromatic ring
JPH08299798A (ja) 改良還元アミノ化触媒
JP2003516225A (ja) アルキン及びジエンの選択水素化担持触媒
EP1412310B1 (de) Verfahren zur hydrierung von aromatischen verbindungen mit restgas enthaltendem wasserstoff
WO2020049502A1 (en) Copper-based catalysts
WO2002030855A1 (de) Verfahren zur hydrierung von aromaten mittels reaktivdestillation
ZA200510307B (en) Hydrocracking of diphenylalkanes
CN111036204B (zh) 一种甘油氢解方法
US6750374B2 (en) Manufacture of cyclohexane from benzene and a hydrogen source containing impurities
CN112138704A (zh) 二次煅烧球磨法制备异丁烷脱氢催化剂的方法和由该方法得到的异丁烷脱氢催化剂及应用
JPS6256788B2 (zh)
WO2018080333A1 (en) Process for production of acrylic acid, process for the selective oxidation of carbon monoxide, catalyst for the selective oxidation of carbon monoxide, process for producing the same
EP1754535A1 (en) Process for hydrogenating acetylenes
CN112573980B (zh) 一种制备异丙苯的方法及其异丙苯、以及环氧丙烷的制备方法
WO2001010802A1 (en) Manufacture of cyclohexane from benzene and a hydrogen source containing impurities
CN116940414A (zh) 催化剂和环戊烯的制造方法
JP2005097231A (ja) ナフトール類の水素化物の製造方法

Legal Events

Date Code Title Description
C06 Publication
PB01 Publication
C10 Entry into substantive examination
SE01 Entry into force of request for substantive examination
C02 Deemed withdrawal of patent application after publication (patent law 2001)
WD01 Invention patent application deemed withdrawn after publication

Application publication date: 20110907