CN1364151A - 催化气相氧化制得马来酸酐的方法 - Google Patents
催化气相氧化制得马来酸酐的方法 Download PDFInfo
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- CN1364151A CN1364151A CN01800039A CN01800039A CN1364151A CN 1364151 A CN1364151 A CN 1364151A CN 01800039 A CN01800039 A CN 01800039A CN 01800039 A CN01800039 A CN 01800039A CN 1364151 A CN1364151 A CN 1364151A
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- reactor
- heat exchanger
- exchange medium
- exchanger plate
- heat exchange
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- Chemical & Material Sciences (AREA)
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- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Materials Engineering (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Furan Compounds (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
Abstract
一种在反应器中通过非均相催化的气相氧化制备马来酸酐的方法,在反应器一端加反应混合物,在反应器相对一端卸下产物混合物,该反应器还有反应热的消散设备,该设备安排在反应器内,热交换介质流过该设备,并且该设备设计成热交换器板。
Description
发明领域
本发明涉及一种采用多相催化的气相氧化制备马来酸酐的方法。
背景技术
马来酸酐有很大的工业重要性。例如,它可以用于缩合聚合和加成聚合,聚酯树脂和醇酸树脂是最重要的工业副产物。另外,马来酸酐是商业上重要化学品的原料,例如琥珀酸酐、γ-丁内酯、1,4-丁二醇和四氢呋喃。
在已知的气相氧化得到马来酸酐的工业规模方法中,含有正-丁烷、氧以及例如氮和蒸汽之类组分的反应混合物,在320-480℃下,在由单个颗粒组成的催化剂床中可转化成反应混合物,除基本组分马来酸酐之外,该混合物还含有蒸汽、一氧化碳、二氧化碳、未反应的丁烷、惰性气体,例如氮气,还含有有机痕量组分。在该过程中释放的反应焓加热了反应混合物。强烈加热该反应混合物因无选择的过氧化作用而降低希望的有价值的产物马来酸酐的产率,非常强烈的加热可带来在气相中这种反应变成燃烧反应的危险,还大大提高了温度和压力。
为了能制约温度增加,一些反应焓于是通过催化剂周围的反应器壁消散在使用的反应器中。为此目的,反应空间分成大量平行的单个反应空间,这些空间呈内径20-45毫米的管状。反应混合物从顶部通过垂直的单个管子流到底部,这些管子被催化剂床填充,60%以上反应焓通过管壁释放到在管周围流过的热-交换介质中。使用的热交换介质一般是无机盐熔体,但也可能使用有机热交换介质、金属熔体或气体,例如氦气。为了将反应器中热交换介质的加热限制在20℃以下,高循环量和相应的泵容量是必不可少的。通常可以在热交换介质通过或在其周围流过的管中产生蒸汽,实现热交换流体的再冷却。
对于高选择性反应,必须将反应管中的轴向和径向温度梯度限制在30℃以下。对于轴向温度梯度,在反应混合物被加热到反应温度的反应器管中内预热区域仍不予考虑,而该反应管也可以定位在实际反应器的热交换器上游。最大允许的径向温度梯度决定了最大管直径,而在充填催化剂床的管中,充足的对流传热所必需的最小气体速度,连同特定的反应速率决定了最小管长度。为了满足这些要求,每年生产约30000公吨马来酸酐的工业规模方法使用的反应器装有12000-40000根平行连接的反应管。最短的反应管长度和最小的气体速度又造成反应器上流动压力损失高于0.4巴。为了避免不均匀流入反应管,因此避免相应的选择性损失,还避免因局部过热而完全变成在气相中均匀燃烧反应的危险,大量反应管的每根管中的压力损失因此通常以非常复杂的方式调平衡。在反应中催化剂的装卸因此是非常费时的,也是费钱的。
因此,这类反应器首先一个缺陷是,必需有非常大量的单个反应管,因此导致设计复杂,成本高。另外一个缺陷是必需有装热交换介质的中间回路,这又意味着必需有高泵容量,以及为再冷却热交换介质而带来的附加成本。此外,出现放热的损失。另外一个缺陷是在单个反应管中高压损失和必需的调平衡,因此,导致非常复杂的催化剂处理。
DE-C-197 54 185描述了例如一种反应器,该反应器有一个圆柱反应器槽,该槽有热板状的热交换器板,而这些板在垂直取向的反应器槽中以彼此预先确定的间隔并排地排列在反应器的开孔基座上。冷却介质通过在槽盖区域的适当设备加到热交换器板,并且通过在槽底区域的适当设备从热交换器板排出,这样该冷却介质流过这些板。气体反应介质与冷却介质逆流在热交换器板之间通过,在槽底区域加料,而在槽盖区域卸料。该说明书绝对没有给出有关这类反应器可以用于多相催化气相氧化得到马来酸酐的任何提示。
DE-A-197 19 375描述了一种在反应器中用氧催化气相氧化乙烯制备环氧乙烷的方法,其中催化剂安排在热交换器板之间的反应区域中,而气体反应混合物流过催化剂。在催化气相氧化得到环氧乙烷时,每个体积单位的催化剂放出了比较少量的热量。
发明概述
本发明的一个目的是提供一种马来酸酐的制备方法,该方法具有增加的经济效益,特别是热交换介质的消耗,甚至以非常高的转化率和使用大容量设备尤其如此。
我们已发现,通过在热交换器板之间的反应空间,因此在提供超过反应器截面的二-维催化剂床中进行非均相催化气相氧化得到马来酸酐,可以达到这个目的。令人惊奇地,这里已发现生成马来酸酐的选择性非预见性地增加。
因此,本发明涉及一种在反应器中通过非均相催化的气相氧化制备马来酸酐的方法,在反应器一端为反应混合物加料端,在反应器相反一端为产物混合物卸料端,该反应器还有反应热的消散设备,该设备安装在反应器内,并且热交换介质流过该设备,其中该设备是热交换器板。
具体实施方案的详细描述
在下面的说明书、附图和附属的权利要求书中说明了本发明的优选实施方案。
使用的原料化合物在原则上可以是制备马来酸酐的任何已知原料,特别是正-丁烷、正-丁烯或它们的混合物、苯或丁二烯。最优选的是用正-丁烷制备。有利地用分子氧或含分子氧的气体,例如空气进行催化气相氧化,空气是特别优选的。另外,反应混合物还可以含有其他组分,例如氮气、蒸汽或其他惰性化稀释气体,例如二氧化碳、一氧化碳、异丁烷和/或甲烷。
气相氧化优选地在温度320-480℃,特别地在380-450℃下,并且在适当超大气压,优选地在1-6巴的绝对压力下进行。
可能的是使用在制备马来酸酐现有技术领域里已知的任何非均相催化剂。优选的非均相催化剂是以钒和磷氧化物为主要成分的氧化多组分催化剂(所谓的V-P-O催化剂),例如(VO)2P2O7。这些催化剂可以与助催化剂混合,例如锌、锆、铋、锑、锡、镍、钴、铁、铬、锰和/或钼。使用苯作为原料化合物时,使用以钒和钼氧化物为主要成分的催化剂也是可能的。催化剂的形状不受任何特别的限制。可以使用含有单个颗粒并且有孔的任何固体几何形状。催化剂颗粒例如可以是圆柱、长方体、圆锥、棱柱形、锥体或三叶形形状。该催化剂优选地由水压直径为3-8毫米的单个颗粒组成。该催化剂也可以呈载带催化剂形式,例如像在DE-A-2 351 151中所描述的,其中将催化活性材料涂布在惰性载体上。同时使用不同活性和/或不同形状的催化剂也是可能的,这里为了比较好地控制催化剂的性能,也可以往反应混合物中加入少量磷化合物,特别是有机磷化合物。使用具有不同尺寸的催化剂颗粒,或附加地使用惰性固体材料作为稀释剂,也可以控制催化剂的性能。
合适的反应混合物含有0.5-10%(体积)上述原料化合物、6-30%(体积)氧和余量为其他组分,例如氮气、蒸汽和/或其他惰性化稀释气体,特别是如前面定义的惰性化稀释气体,在每种情况下,都以100%(体积)反应混合物计。
C4原料化合物的催化气相氧化没有得到纯的马来酸酐,而得到产物混合物,除了马来酸酐外,该混合物含有例如乙酸、丙烯酸、巴豆酸、一氧化碳、二氧化碳、未反应的原料化合物等第二组分。在以产物混合物作为整体为基的每种情况下,该产物混合物通常含有0.2-4%(体积)马来酸酐、0.01-0.09%(体积)乙酸和/或丙烯酸中的每一种,以及余量为氮气、二氧化碳、一氧化碳、蒸汽和/或其他惰性化稀释气体。在氧化苯时,有少量苯醌、甲醛和甲酸副产物。
反应器形状原则上不受任何限制。可以使用通常的圆柱反应器,但也可以使用长方体反应器。对于反应器的取向同样没有任何限制;反应器原则上可以任何位置取向,对于圆柱反应器的特定情况,垂直取向一般是优选的。
根据本发明,有设计成热交换器板的消散反应热的设备的反应器,用于气相氧化得到马来酸酐的方法。在本发明的优选实施方案中,反应器释放的至少60%反应焓通过热交换器板消散掉。一些反应焓也可以随反应气体消散掉,或在反应器中以通常的方式提供部分热交换表面积。在这种情况下,部分热交换表面积还可以被气体间隔(中间冷凝器)或惰性材料(预热区域,第二个冷凝器)围绕。
热交换器板主要是二-维结构,它们有与表面积相比厚度很小的内部空间,这种空间提供了加料和卸料管线。它们一般是用金属板,经常用钢板制成。但是,取决于应用,特别是取决于反应介质和热交换介质的性质,可以使用特殊的,尤其是耐腐蚀的材料。热交换介质的加料和卸料设备一般安排在热交换器板的相对端。热交换器板优选地由至少两块其周边以耐压密封方式连接的金属板组成,这些板用15-80毫米栅格通过点连接,优选地通过点焊使彼此相互支撑,并且通过内压膨胀,热交换介质则流过以这种方式构成的内部空间。在特别优选的实施方案中,热交换器板的宽度是0.5-3米,最大长度是8米,而总厚度是5-100毫米。在另一个优选实施方案中,由至少四块单板以这样的方式构造热交换器板,以致形成围绕中心袋的两个优选充气绝热袋,而热交换介质流过该中心袋。
关于在反应器中热交换器板的排列,原则上没有没有任何限制;热交换器板在反应器中例如可以呈螺旋形、同心或径向排列。它们也可以悬挂在反应器套管中。优选地,它们层叠得到平面-平行的预装件,再弯曲得到环或环段,然后同心排列,或以螺旋方式弯曲,板之间优选余下的中间间隔为至少4毫米,至多60毫米。还可能的是将板的预装件置于倾斜,这里至少一个板预装件以这样的方式排列,以致由这些板形成的流动通道与反应器的中心轴构成0-20°角。热交换器板的表面直到催化剂层也可以有隔离物,这种隔离物优选地是用膨胀的金属筛网或惰性材料实现的。另外,单个板预装件可以在不同的热交换介质温度下操作,而温度沿反应器轴改变。这类温度分区能够与不同的热流密度匹配。此外,单个板预装件在流动方向的板分开度可以随反应不断进行,表观密度降低而增加,这样补充和/或代替上述的温度分区。
使用具有楔形的热交换器板,即热交换介质流过它们的内表面优选地沿反应混合物流的方向连续减少,也是有利的。例如可以把两块板放在一起,并以不断增加的分开度的方式将它们焊接起来,就生产出这类楔形热交换器板。接着把板夹到容易翻转的吹气设备中,并且吹足至预确定的分开度。使用以楔形构成的热交换器板可以优化与反应温度分布的匹配。在另一个有利的实施方案中,热交换器板可以在其全部或部分长度上焊接起来。为此,在每种情况下,放置两个板,使一个板置于另一个板顶上,整个纵向缝采用辊缝焊进行焊接,再用适当的吹气设备吹足。
根据另外一个实施方案,把相互平行取向的平面矩形板如此放入反应器内,以致它们基本上完全装满反应器,这里每块板两个相对边的边缘在同一方向以直角切成斜角,在接下的各个板中,其他两个相对边的边缘以同样的分开度在同一方向以直角切成斜角,以便在每种情况下构成长方体空间,反应混合物或热交换介质以横向环流流过各自相邻空间。
根据另外一个实施方案,热交换器板沿反应器纵向方向相互平行排列。
在另一个实施方案中,以这样的方式偏移板预装件,以致板的横向轴取向在至少两个连续的板预装件之间相差0-90°。
在本发明方法中可以使用的热交换介质原则上没有任何限制。可能的是使用在催化气相氧化反应温度下,仍呈液体物理状态,或者部分或全部蒸发的无机和有机液体热交换介质。例如,盐熔体是特别合适的。此外,使用气体热交换介质也是可能的,优选的是氦气。使用在催化气相氧化反应温度下完全或至少部分地蒸发的热交换介质是特别有利的。对于这种目的,水是特别优选的。利用蒸发冷却,这里可保证有效的热消散,与使用不改变物理状态的热交换介质相比,要达到消散同样量的热量,可大大节省必需的热交换介质量。在一个优选实施方案中,高沸点的物质,优选多元醇加到热交换介质中,其目的是提高沸点,或者使用纯的醇。
可以并流或逆流两种方式进行蒸发冷却。在与下面流入并流操作的情况下,另外可能的是以这样的方式调节沸腾液体的水平,以致向反应器端部进行低热消散,并且在这里现在较高温度水平造成总产率增加。在蒸发冷却的情况下,根据温度,在冷却介质侧,一定的蒸汽压(在水的情况下,其值是约20-160巴)变成是确定的,使得在装置冷却介质侧的相应耐压密封设计必不可少。
在本发明另外的优选实施方案中,呈泡、滴和/或气溶胶状的热交换介质蒸汽和液体的混合物流过热交换器板。可以特地喷入足够的热交换介质,使得基本上通过气相进行传热,因此有意地减少该介质。
根据本发明,将在反应器一端的反应混合物加到在热交换器板之间的反应器内部空间中,并在反应器相对端排出。因此,反应混合物通过热交换器板之间的空间流过反应器。于是,反应混合物进行持续的相互混合,其结果为反应混合物的高度均匀性。
热交换介质与反应混合物可以并流、逆流或错流方式通过反应器。并流方式是特别优选的,因为这样能够保证更好地与反应温度分布匹配。
根据另一个优选实施方案,可以沿反应混合物流的方向排列两个或两个以上具有分开热交换介质回路的反应区域。
催化剂可以例如以无序床形式加入热交换板之间的空间中。与采用已知方法加入反应管相比,加入或更换催化剂床在这种情况下是比较简单和比较均匀的。形成了较大的连贯反应空间,并且催化剂床的堵塞危险性也降低了。在催化剂安放在热交换器板周围的床中的情况下,有利的是,在局部断层的情况下,反应气体本身在流过其限制之后在两个热交换器板之间的整个催化剂截面上再次重新分配,并且整个反应截面有助于转化。热交换器板的另一个优点是,在更换催化剂的情况下,比管-束式反应器更易于腾空催化剂。
但是,除了催化剂床外或作为催化剂床的另一种选择,提供在其反应混合物流过的外表面上带催化涂层的热交换器板也是可能的。在这种情况下,将该催化剂直接涂到板上,其层厚为0.1-1.5毫米。优选地,待涂板可采用如喷砂、喷球的机械方法或如蚀刻或预涂布的化学方法进行预处理。由于热交换器板表面为基本平的形状,与反应管相比,涂布它们更简单。
因此,本发明的方法包括下述特征和优点。
-使用可替换的热交换器板,设计简单;这些板可使用标准化板,因此可以进一步节约成本;
-耐高压能够通过产生新汽而选择性冷却,也不需要任何中间回路,因此低比热交换介质的处理能力和较低的泵容量以及降低的放热损失;
-广义来说,催化剂在反应器(连续床)中呈“均匀相”形式,它能够使压力、温度和组成达到相互平衡;这就导致很少生成“热流通道”,因此抑制了反应器中最高温度,所谓的热点,另外还导致在反应器中的较低压力损失,从而使得已知方法中使用的单个反应管平衡不是必需的;
-催化剂的处理大大简化;从简单装反应器到上述最高的板预装件预备区域或保护床都是可能的。
下面参看代表本发明优选实施方案的附图将更详细地解释本发明。
在附图中,相同或相应的零件使用相同的参考编号。
图1表示一个特别适合实施本方法的特别优选反应器实施方案的纵向剖面图,
图1a表示图1反应器的横剖面图,
图1b表示图1反应器中热交换器板的纵向剖面图,
图1c表示图1b热交换器板上优选排列的焊点,
图2表示一个特别适合实施本方法的反应器纵向剖面图,而反应混合物与热交换介质并向流动,
图3表示一个特别适合实施本方法的另外优选的反应器实施方案的纵向剖面图,而反应混合物与热交换介质逆向流动,
图4表示适合实施本方法的长方体反应器纵向剖面图,
图4a表示图4中示出反应器的放大剖面图,以便说明反应器板结构,
图4b表示图4示出的反应器横向剖面图,以及
图5表示适合实施本方法的反应器纵向剖面图,作为实例,所述反应器具有三个反应区域。
图1中以纵向截面显示的反应器为圆柱形状,在上部区域加反应混合物(1),在反应器下部区域卸下产物混合物(2)。反应混合物(1)通过催化剂床(5)。热交换板(8)为楔形设计,这些板以反应器纵向方向排列在反应器内部空间中。热交换介质通过加料(3)和分配管线(6)加料,而通过收集管线(7)和卸料管线(4)卸料,该热交换介质流过反应器板。图1a中的横向剖面图说明了热交换器板(8)的基本平行排列。
图1b和1c说明了热交换器板(8)的楔形设计,它们采用彼此点焊接的板构成。
图2作为实例说明有并流流动的反应混合物和热交换介质的反应器纵向剖面图。图2清楚地表明热交换器板(8)中的热交换介质液面只是达到一定高度,即热交换介质在这个液面上蒸发。采用蒸发冷却可进行热消散。
图3作为实例说明以逆流流动的反应混合物和热交换介质。
图4说明长方体反应器的纵向剖面图;在图4a放大说明的剖面图中,清楚地显示热交换器板(8)的设计。图4b说明在图4a中示出的长方体反应器的横向剖面图。
作为实例,在图5中以纵向剖面表示的反应器有三个反应区,每个反应区有分开的热交换介质回路。
Claims (9)
1、一种在反应器中通过非均相催化的气相氧化制备马来酸酐的方法,在反应器一端加反应混合物(1),在反应器相对一端卸料(2),该反应器还有反应热的消散设备(8),该设备安排在反应器内,并且热交换介质流过该设备,其中该设备(8)是热交换器板。
2、根据权利要求1所述的方法,其中使用在流过热交换器板(8)时至少部分蒸发的液体热交换介质。
3、根据权利要求1或2所述的方法,其中热交换器板由至少两块其周边以耐压密封方式连接的金属板组成,这些板用15-80毫米栅格通过点连接,优选地通过点焊使彼此相互支撑,并且通过内压膨胀,热交换介质则流过以这种方式构成的内部空间。
4、根据权利要求3所述的方法,其中热交换器板层叠得到平面-平行的预装件,再弯曲得到环或环段,然后同心排列,或以螺旋方式弯曲。
5、根据权利要求4所述的方法,其中单个板预装件的板分开度可以在随着反应不断进行,相应表现密度降低的流动方向而增加。
6、根据上述权利要求中任一权利要求所述的方法,其中使用液体的无机或有机热交换介质或气体热交换介质。
7、根据上述权利要求中任一权利要求所述的方法,其中热交换器板(8)安排成相互平行。
8、根据上述权利要求中任一权利要求所述的方法,其中面向反应混合物的热交换器板的表面具有完全或部分的催化剂涂层。
9、根据上述权利要求中任一权利要求所述的方法,其中反应混合物含有正丁烷、氧以及,如果需要的话,其他组分。
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DE10000584A DE10000584A1 (de) | 2000-01-10 | 2000-01-10 | Verfahren zur katalytischen Gasphasenoxidation zu Maleinsäureanhydrid |
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EP (1) | EP1185494B1 (zh) |
JP (1) | JP2003519673A (zh) |
KR (1) | KR100703915B1 (zh) |
CN (1) | CN1208300C (zh) |
AT (1) | ATE238265T1 (zh) |
AU (1) | AU4232901A (zh) |
BR (1) | BR0103915A (zh) |
DE (2) | DE10000584A1 (zh) |
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Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN103028350A (zh) * | 2012-12-06 | 2013-04-10 | 浙江大学 | 用于正丁烷氧化制顺酐的固定床反应器及其方法 |
CN103071433A (zh) * | 2013-01-17 | 2013-05-01 | 浙江大学 | 用于正丁烷氧化制顺酐的固定床反应器的气体预分布器 |
Families Citing this family (17)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US6903047B2 (en) * | 2000-01-20 | 2005-06-07 | E.I. Du Pont De Nemours And Company | Vanadium-phosphorus oxide catalysts with promoter reagents |
EP1350560A1 (en) * | 2002-04-05 | 2003-10-08 | Methanol Casale S.A. | Plate-type heat exchange unit for catalytic bed reactors |
DE10215778A1 (de) * | 2002-04-10 | 2003-12-18 | Basf Ag | Reaktor zur thermischen Spaltung von mono- und polyfunktionellen Carbamidsäureestern |
JP4212888B2 (ja) * | 2002-12-26 | 2009-01-21 | 三菱化学エンジニアリング株式会社 | プレート型触媒反応器 |
TWI338590B (en) * | 2003-07-24 | 2011-03-11 | Basf Ag | Preparation of (meth)acrolein and/or (meth)acrylic acid by heterogeneously catalyzed partial oxidation of c3 and/or c4 precursor compounds in a reactor having thermoplate modules |
US7410622B2 (en) * | 2003-07-24 | 2008-08-12 | Basf Aktiengesellschaft | Reactor for partial oxidations having thermoplate modules |
KR101196082B1 (ko) * | 2003-12-23 | 2012-11-01 | 바스프 에스이 | 써모플레이트를 사용하여 반응기 내에서의 유체 반응혼합물의 반응을 모니터링, 제어 및(또는) 조절하는 방법 |
GB0509746D0 (en) * | 2005-05-13 | 2005-06-22 | Ashe Morris Ltd | Variable plate heat exchangers |
TW200719968A (en) * | 2005-10-31 | 2007-06-01 | Sued Chemie Ag | Catalyst molding for partial oxidation reactions |
DE102009031765B4 (de) * | 2009-06-25 | 2012-10-11 | Chemieanlagenbau Chemnitz Gmbh | Konverter zur Durchführung exothermer katalytischer Reaktionen |
JP5457145B2 (ja) * | 2009-11-20 | 2014-04-02 | 川重冷熱工業株式会社 | 流体加熱装置 |
US9073034B2 (en) | 2010-03-17 | 2015-07-07 | Dow Technology Investments Llc | Efficient fixed bed platform for production of ethylene oxide by partial oxidation of ethylene using catalyst of wide selectivity |
DE102010050152B4 (de) * | 2010-11-02 | 2016-02-11 | Adam Handerek | Reaktor und Verfahren zum zumindest teilweisen Zersetzen, insbesondere Depolymerisieren, und/oder Reinigen von Kunststoffmaterial |
DE202011050657U1 (de) * | 2011-07-07 | 2012-10-09 | Deg Engineering Gmbh | Reaktor für die katalytische Umsetzung von Reaktionsmedien |
US9440903B2 (en) * | 2012-09-24 | 2016-09-13 | Arkema Inc. | Shell and tube oxidation reactor with improved resistance to fouling |
CN109012509A (zh) * | 2018-09-29 | 2018-12-18 | 宁波浙铁江宁化工有限公司 | 顺酐制备反应器中的熔盐循环结构 |
CN112044363B (zh) * | 2020-08-31 | 2022-09-13 | 江苏永大化工机械股份有限公司 | 煤制乙二醇生产用偶联反应器 |
Family Cites Families (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE2016614A1 (en) * | 1970-04-08 | 1971-10-21 | Badische Anilin & Soda Fabrik AG, 6700 Ludwigshafen | Exothermic oxidation in catalytic reactor |
US4077912A (en) | 1972-10-12 | 1978-03-07 | Standard Oil Company | Catalysts useful for exothermic reactions |
FR2536676B1 (fr) * | 1982-11-26 | 1993-01-22 | Inst Francais Du Petrole | Reacteurs a plaques pour syntheses chimiques effectuees sous haute pression en phase gazeuse et en catalyse heterogene |
DE19719375A1 (de) | 1997-05-07 | 1998-11-12 | Linde Ag | Verfahren und Reaktor zur Herstellung von Ethylenoxid |
DE19754185C1 (de) | 1997-12-06 | 1999-02-04 | Deg Engineering Gmbh | Reaktor für die katalytische Umsetzung von Reaktionsmedien, insbesondere von gasförmigen Reaktionsmedien |
DE19857842A1 (de) | 1998-12-15 | 2000-06-21 | Basf Ag | Reaktormodul mit einem Kontaktrohrbündel |
JP2001038195A (ja) * | 1999-06-28 | 2001-02-13 | Basf Ag | 熱交換板を備えた反応器 |
DE19952964A1 (de) | 1999-11-03 | 2001-05-10 | Basf Ag | Verfahren zur katalytischen Gasphasenoxidation zu (Meth)Acrolein und/oder (Meth)Acrylsäure |
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2000
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Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN103028350A (zh) * | 2012-12-06 | 2013-04-10 | 浙江大学 | 用于正丁烷氧化制顺酐的固定床反应器及其方法 |
CN103071433A (zh) * | 2013-01-17 | 2013-05-01 | 浙江大学 | 用于正丁烷氧化制顺酐的固定床反应器的气体预分布器 |
CN103071433B (zh) * | 2013-01-17 | 2016-04-13 | 浙江大学 | 用于正丁烷氧化制顺酐的固定床反应器的气体预分布器 |
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US6624315B2 (en) | 2003-09-23 |
DE10000584A1 (de) | 2001-07-12 |
KR100703915B1 (ko) | 2007-04-05 |
US20020161243A1 (en) | 2002-10-31 |
WO2001051448A2 (de) | 2001-07-19 |
ES2198397T3 (es) | 2004-02-01 |
MY127153A (en) | 2006-11-30 |
AU4232901A (en) | 2001-07-24 |
EP1185494B1 (de) | 2003-04-23 |
ATE238265T1 (de) | 2003-05-15 |
WO2001051448A3 (de) | 2001-12-27 |
EP1185494A2 (de) | 2002-03-13 |
JP2003519673A (ja) | 2003-06-24 |
DE50100187D1 (de) | 2003-05-28 |
BR0103915A (pt) | 2001-12-18 |
CN1208300C (zh) | 2005-06-29 |
KR20010102538A (ko) | 2001-11-15 |
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