CN102105563A - 纯化包含乙烯的废气进料流的工艺 - Google Patents
纯化包含乙烯的废气进料流的工艺 Download PDFInfo
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- 238000000034 method Methods 0.000 title claims abstract description 38
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- 239000010931 gold Substances 0.000 claims description 4
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- MCMNRKCIXSYSNV-UHFFFAOYSA-N Zirconium dioxide Chemical class O=[Zr]=O MCMNRKCIXSYSNV-UHFFFAOYSA-N 0.000 claims description 3
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- JCXGWMGPZLAOME-UHFFFAOYSA-N bismuth atom Chemical compound [Bi] JCXGWMGPZLAOME-UHFFFAOYSA-N 0.000 claims description 3
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- 239000010949 copper Substances 0.000 claims description 3
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Abstract
公开了一种用于纯化来自蒸汽裂化装置或流化催化裂化装置(FCC)中的包含乙烯的进料流的方法，其中进料流还包含氢气、一氧化碳、乙炔类、氧气、氮的氧化物。该方法包括在至少120℃的反应温度下使包含乙烯的气流与Ru基催化剂接触。该工艺产生包含乙烯的进料流，其中乙烯基本上不含乙炔类、氮的氧化物和氧气。以乙烯的损失最少来进行进料流的纯化。
Description
技术领域
本进展是可以用于纯化来自蒸汽裂化装置或流化催化裂化装置(FCC)的未净化气体流或废气流的方法。通过本进展的方法，使用负载型钌基催化剂可以从包含乙烯、氢气和CO的未净化气体进料流中同时去除乙炔、甲基乙炔、氮的氧化物和氧气，而不会显著损失乙烯。催化剂可以包含分布到选自氧化铝或其他通常已知的催化剂载体材料的载体上的0.01wt.％到5wt.％的钌。
背景技术
诸如流化催化裂化(FCC)和深度催化裂化(DCC)的催化裂化工艺多年来已经广泛用在工业内来生产运输燃料，诸如汽油和柴油。来自FCC和DCC工艺的废气包含诸如乙烯和丙烯的有价值的产物。然而，这些废气流包含相对稀浓度的烯烃且通常被认为由诸如分馏的常规方法回收烯烃在商业上是不可行的。因而，大多数炼油厂使用废气作为燃料气体。
最近，从废气流中回收这些相对高价值的烯烃得到了越来越多的关注。例如，美国专利5,981,818描述了一种用于从废气中回收稀的烯烃的方法。除了有价值的烯烃外，FCC/DCC还包含诸如乙炔类和二烯烃的有害杂质。需要从废气流中去除这些杂质以便在下游工艺中利用高价值的烯烃。通常，在商业上由选择性氢化工艺来去除存在于烯烃流中的乙炔类和二烯类。
大多数商业化规模的选择性乙炔氢化操作使用钯基催化剂。除了烃之外，废气流通常包含氮的氧化物、氧气、硫和其他杂质。Pd基催化剂对乙炔和二烯类的选择性氢化具有高的活性和选择性；但它们对硫和其他一些毒物非常敏感。而且，已知Pd基催化剂用于去除氮的氧化物和/或氧气不是特别有效。
镍催化剂也已经用于乙炔和二烯类的选择性氢化。镍催化剂是耐硫中毒的，但对乙炔的氢化不是选择性的。更通常来说，虽然去除了乙炔，但大量的烯烃也被氢化成饱和烃。当进料气流中的一氧化碳水平高时，尤其是在低温下时，镍基催化剂还倾向于形成羰基镍。羰基镍是高挥发性的、高毒性的物质，可沉积在下游装置中并对那个区域的工人带来显著的安全危害。
美国专利2,747,970教导并要求保护一种使用由活化的土金属氧化物，诸如活化氧化铝上的0.01wt.％到2.0wt.％的钌组成的催化剂来从气流中去除一氧化碳和二氧化碳的工艺。该工艺包括将气流与负载型催化剂直接接触，同时保持至少120℃的反应温度，直到将CO和CO2的碳成分基本上完全转化成甲烷。然而，该工艺并未教导相同的催化剂和方法可以用于从乙烯气流中去除乙炔、甲基乙炔、丁二烯、NO和O2且不会有损失乙烯的风险。确实教导使用钌催化剂来纯化乙烯流的现有技术通常将钌催化剂引述为这种应用的低效催化剂的示例。例如，在美国专利4,299,800中，评价了用于从包含乙烯的进料流中去除氧气的、包含氧化铝上0.5wt.％钌的催化剂。在低温(50℃)下，除氧率是低的且基本上检测不到乙烯的转化。然而，与使用氧化铝上的银、金或钒时的小于5％的乙烯转化率相比，在高温(200℃)下，氧去除率达到99.4％，但却伴随着11.2％的乙烯转化(损失)。
因而，存在一种用于从废气流中去除氧气、乙炔类和氮的氧化物的工艺的需求，其中乙烯在纯化工艺期间不会转化成较低价值的烃且其中纯化的包含乙烯的气流包含每一种小于约1ppm的乙炔类、氮的氧化物和氧气。
本发明实施方案的公开内容
在一个实施方案中，描述了一种用于纯化来自蒸汽裂化装置或流化催化裂化装置(FCC)的包含乙烯的进料流的方法，其中进料流还包含氢气、一氧化碳、氮的氧化物、氧气和乙炔类。该方法包括使包含乙烯的气流与Ru基催化剂接触。该工艺产生包含小于约1ppm的乙炔类、小于约1ppm的氮的氧化物和小于约1ppm的氧气的包含乙烯的产物流。以乙烯的损失最少来进行进料流的纯化。
在另一个实施方案中，描述了一种用于从包含乙烯的进料流中去除氧气、乙炔类和氮的氧化物的方法，该包含乙烯的进料流还包含氢气和一氧化碳。该方法包括使包含乙烯的气流与包含分布到载体上的0.01wt.％到5wt.％之间的钌的Ru基催化剂接触以产生基本上不含乙炔类、氮的氧化物和氧气的包含乙烯的产物。
实施本发明实施方案的方式
包含乙烯的进料流可以是来自任何蒸汽裂化装置、流化催化裂化装置或类似工艺的废气流。通常，废气流包含氢气、一氧化碳、氧气、氮的氧化物、乙烷、乙烯和乙炔。
钌基催化剂可以是包含分布到通常的催化剂载体材料上的钌的任何催化剂，催化剂载体材料诸如，但不限于，氧化铝类、二氧化钛类、氧化锆类、二氧化硅类、金属铝酸盐类、硅铝酸盐类、尖晶石类及其组合。制备负载型钌催化剂的方法是本领域众所周知的。任选地，催化剂还可以包含助催化剂，诸如，但不限于，银、金、铜、锌、铋、铅或其组合。在示例性的实施方案中，催化剂包含分布在氧化铝载体上的钌，其中用钌盐溶液将钌分布在载体上。
在一个实施方案中，催化剂包含分布在氧化铝载体上的钌，其中通过用钌盐溶液浸渍氧化铝载体而将钌分布在载体上。催化剂可以包含0.01wt.％到5wt.％之间的钌。在其他实施方案中，催化剂可以包含任何类型的载体(包括氧化铝)上的0.01wt.％到1wt.％的钌，0.1wt.％到0.5wt.％的钌；0.15wt.％到0.30wt.％的钌，最少0.15wt.％的钌或最少0.3wt.％的钌或基本上由任何类型的载体(包括氧化铝)上的这些量的钌组成。
在可选择的实施方案中，催化剂包含分布在氧化铝载体上的钌，其中载体具有至少3m2/g的BET表面积，且优选具有约3m2/g到约200m2/g的BET表面积。可选择地，催化剂可以包含低表面积载体上的钌、中等表面积载体上的钌或高表面积载体上的钌。一般而言，具有1m2/g-10m2/g之间的BET表面积的载体可以归为低表面积载体。中等表面积载体通常在10m2/g-60m2/g之间的范围，而高表面积载体通常具有大于60m2/g的BET表面积。就氧化铝而言，低表面积、中等表面积和高表面积的范围分别是1m2/g-10m2/g、30m2/g-60m2/g和大于60m2/g。在另一个实施方案中，载体是中等表面积氧化铝载体。
在其他实施方案中，以保持在载体的外层上的方式将钌分布到氧化铝载体的外层上。“分布到载体的外层上”意指钌可以位于从载体的任何部分的外表面向载体的中心延伸约300μm距离的任何部分内。分布到载体的外层上的钌的深度可以是恒定的或可以是变化的，特别是在孔位于载体的外表面上的地方。
该工艺包括将气流与负载型催化剂直接接触，同时保持至少120℃的反应温度，直至乙炔含量降到小于一(1)ppm且氮的氧化物含量降到小于一(1)ppm以及氧气含量降到小于一(1)ppm。可选择地，该工艺可以包括使气流与负载型催化剂接触，直到产物流基本上不含杂质，杂质可以包含乙炔、氮的氧化物、氧气及其组合。在其他实施方案中，乙炔、氮的氧化物和氧气含量的去除可以较高或较低，这取决于许多因素，包括约束FCC/DCC工厂的运行和/或工厂设计的法律和法规。
可以使催化剂在使用前还原或硫化。在装载到反应器中之后且在引入包含乙烯的气流之前，催化剂可以通过在至少100℃的温度下将氢气或包含氢气的气体进料通过催化剂至少一分钟来还原。在装载到反应器中之后且在引入包含乙烯的气流之前，催化剂可以通过在至少150℃的温度下将含硫的气流进料通过催化剂至少一分钟来硫化。
工业实用性
上述实施方案可以用于纯化来自蒸汽裂化装置、流化催化裂化装置(FCC)的包含乙烯的进料流或包含氢气、一氧化碳、氧气和乙炔类的任何类型的烃进料流。
实施例
作为代表性的实施例，获得并评价了用于从乙烯进料流中去除杂质的好几种催化剂。提供这些实施例是为了进一步解释本发明，而并不是期望，或用来限制本发明的范围。
所评价的催化剂样品：
催化剂1：市售的Pd基催化剂，OleMax 250；从
-Chemie Inc.，Louisville，Kentucky获得。
催化剂2：低表面积(3.6m2/g)氧化铝载体上的0.15％的钌。
催化剂3：中等表面积(37m2/g)氧化铝载体上的0.15％的钌。
催化剂4：高表面积(165m2/g)氧化铝载体上的0.15％的钌。
催化剂5：高表面积(165m2/g)氧化铝载体上的0.30％的钌。
催化剂样品评价：
在连续流动反应器中通过将约50cc的催化剂装载到反应器中，然后将受污染的包含乙烯的进料流进料通过装载的催化剂来测试所制备的催化剂。基于测试目的，通常将反应器温度调节到约120℃到约300℃的温度，一氧化碳含量控制在约0.05wt.％到5wt.％之间，且硫含量控制在低于约50ppm。氢分压控制在约0.05MPa到2MPa之间且气时空速为约500hr-1到10,000hr-1；更优选地，氢分压控制在约0.10MPa到1MPa之间且气时空速为约1000hr-1到5,000hr-1；以及最优选地，氢分压控制在约0.10MPa到0.3MPa之间且气时空速为约1500hr-1到3500hr-1以及氢浓度为约5％到约15％。
在连续流动反应器中测试催化剂1-4。将约50cc的催化剂装载到反应器内，将反应器温度调节到预定温度(如表1所表示的)，以及将受到氧气、乙炔和一氧化氮污染的包含乙烯的进料流以2500hr-1的气时空速进料通过反应器，同时压力控制在1.9MPa。使用在线气相色谱仪分析反应器入口和出口的气体样品并将结果概述在表1中。
表1
如表1所示，钯催化剂和钌催化剂均有效地将乙烯和氢气保留在气流中，尽管钌催化剂保留了比用钯催化剂所观察到的高的相对百分比的这些气体。此外，钯催化剂和钌催化剂均有效地减少了存在于进料流中的乙炔和氮的氧化物的水平。然而，钌催化剂比钯催化剂明显更有效地去除了进料流中的氧气。而且，更可能是，因为钌催化剂比钯催化剂对乙烯氢化的活性弱，所以当包含乙烯的进料流接触钌催化剂时产生的乙烷比当进料流接触钯催化剂时产生的乙烷少。
在不同反应器温度下，且进料流中存在额外的一氧化碳或硫化氢时，在连续流动反应器中测试了催化剂5。将约50cc的催化剂装载到反应器中，将反应器温度调节到预定温度(如表2所表示的)，以及将受到氧气、乙炔和任选地，一氧化氮或一氧化碳或硫化氢污染的包含乙烯的进料流以2500hr-1的气时空速进料通过反应器，同时压力控制在1.9MPa。使用在线气相色谱仪分析反应器入口和出口的气体样品并将结果概述在表2中。
表2
如表2所示，即使在相对高水平的CO和硫化氢的不利条件下，钌催化剂也有效地将乙烯和氢气保留在气流中。此外，钌催化剂有效地减少了存在于进料流中的乙炔和氧气的水平，并产生相对少量的不期望的乙烷。
因而，通过在控制在至少约120℃的温度下的含有催化剂的连续流动反应器中使还包含氢气、一氧化碳、氧气、乙炔和一氧化氮的包含乙烯的进料流与负载型钌催化剂接触，其中该催化剂包含0.01wt.％到5wt.％之间的钌，可以从气流中去除乙炔类、氮的氧化物和氧气且损失的乙烯最少。
应理解，本领域的技术人员可以改变本文中所显示和描述的实施方案而不偏离本发明的范围。例如，预期本领域的技术人员可以调节反应器压力和气时空速以适应不同尺寸的反应器。
Claims (20)
1.一种用于从包含乙烯的气流中纯化乙烯的方法，所述包含乙烯的气流还包含乙炔类、氧气和氮的氧化物，所述方法包括使所述包含乙烯的气流与包含0.01wt.％到5wt.％之间的钌的负载型钌催化剂接触，直到所述气流包含小于约1ppm的乙炔类、小于约1ppm的氮的氧化物和小于约1ppm的氧气。
2.如权利要求1所述的方法，其中在接触所述气流之前，将所述负载型钌催化剂加热到至少约120℃的温度。
3.如权利要求1所述的方法，其中所述气流在连续流动反应器中与所述催化剂接触。
4.如权利要求3所述的方法，其中所述反应器被保持在120℃到300℃的温度下。
5.如权利要求3所述的方法，其中所述反应器具有0.05MPa到2MPa之间的氢分压。
6.如权利要求1所述的方法，其中所述气流具有500hr-1到10,000hr-1的气时空速。
7.如权利要求5所述的方法，其中所述反应器具有0.10MPa到1MPa之间的氢分压。
8.如权利要求6所述的方法，其中所述气流具有1000hr-1到5000hr-1的气时空速。
9.如权利要求1所述的方法，其中所述钌被负载到选自由氧化铝类、二氧化钛类、氧化锆类、二氧化硅类、金属铝酸盐类、硅铝酸盐类、尖晶石类及其组合组成的组的载体上。
10.如权利要求1所述的方法，其中所述负载型钌催化剂还包含助催化剂。
11.如权利要求10所述的方法，其中所述助催化剂选自由银、金、铜、锌、铋、铅或其组合组成的组。
12.如权利要求1所述的方法，其中所述负载型钌催化剂被还原。
13.如权利要求1所述的方法，其中所述负载型钌催化剂被硫化。
14.一种用于从包含乙烯的气流中纯化乙烯的方法，所述包含乙烯的气流还包含乙炔类、氧气和氮的氧化物，所述方法包括：
(a)用负载型钌催化剂装载连续流动反应器，其中所述催化剂包含0.01wt.％到5wt.％之间的钌；
(b)在所述反应器内将所述催化剂加热到至少120℃的温度；
(c)在0.05MPa到2MPa之间的氢分压下将所述包含乙烯的气流进料到所述反应器内，使得所述气流与所述催化剂接触；以及
(d)当所述气流包含小于约1ppm的乙炔类、小于约1ppm的氮的氧化物和小于约1ppm的氧气时，使所述包含乙烯的气流离开所述催化剂。
15.如权利要求14所述的方法，其中所述反应器被保持在120℃到300℃的温度下。
16.如权利要求14所述的方法，其中所述气流具有500hr-1到10,000hr-1的气时空速。
17.如权利要求14所述的方法，其中所述钌被负载到选自由氧化铝、二氧化钛、氧化锆、二氧化硅、金属铝酸盐类及其组合组成的组的载体上。
18.如权利要求14所述的方法，其中所述负载型钌催化剂还包含助催化剂，所述助催化剂选自由银、金、铜、锌、铋、铅或其组合组成的组。
19.如权利要求14所述的方法，其中在步骤(a)之后且在步骤(b)之前，同时在所述反应器内，在氢气或包含氢气的气体中，在至少100℃的温度下，还原所述催化剂至少一分钟。
20.如权利要求14所述的方法，其中在步骤(a)之后且在步骤(b)之前，同时在所述反应器内，在含硫的气流中，在至少150℃的温度下，硫化所述催化剂至少一分钟。
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- 2009-08-21 WO PCT/US2009/054592 patent/WO2010022318A2/en active Application Filing
- 2009-08-21 EA EA201170071A patent/EA023914B9/ru unknown
- 2009-08-21 ES ES09808863.6T patent/ES2686597T3/es active Active
- 2009-08-21 CN CN2009801287167A patent/CN102105563B/zh active Active
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| US6080905A (en) * | 1997-03-10 | 2000-06-27 | Bp Amoco Corporation | Olefin purification by adsorption of acetylenics and regeneration of adsorbent |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN107847859A (zh) * | 2015-07-13 | 2018-03-27 | 瓦克化学股份公司 | 从包含烃和氧气的气体混合物中去除氧气的方法 |
Also Published As
| Publication number | Publication date |
|---|---|
| EP2318482A2 (en) | 2011-05-11 |
| WO2010022318A3 (en) | 2010-06-10 |
| ES2686597T3 (es) | 2018-10-18 |
| EP2318482B1 (en) | 2018-08-08 |
| WO2010022318A8 (en) | 2012-11-15 |
| US8426660B2 (en) | 2013-04-23 |
| CN102105563B (zh) | 2013-12-04 |
| US20100048972A1 (en) | 2010-02-25 |
| EA023914B9 (ru) | 2016-09-30 |
| WO2010022318A2 (en) | 2010-02-25 |
| EP2318482A4 (en) | 2014-08-06 |
| EA023914B1 (ru) | 2016-07-29 |
| EA201170071A1 (ru) | 2011-08-30 |
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