CN201276506Y - Catalytic reaction dehydrogenation reactor for aromatic satisfied hydrocarbon - Google Patents
Catalytic reaction dehydrogenation reactor for aromatic satisfied hydrocarbon Download PDFInfo
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- CN201276506Y CN201276506Y CNU2008201513828U CN200820151382U CN201276506Y CN 201276506 Y CN201276506 Y CN 201276506Y CN U2008201513828 U CNU2008201513828 U CN U2008201513828U CN 200820151382 U CN200820151382 U CN 200820151382U CN 201276506 Y CN201276506 Y CN 201276506Y
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- 238000006356 dehydrogenation reaction Methods 0.000 title claims abstract description 12
- 125000003118 aryl group Chemical group 0.000 title claims abstract description 8
- 238000006555 catalytic reaction Methods 0.000 title claims description 5
- 229930195733 hydrocarbon Natural products 0.000 title description 4
- 150000002430 hydrocarbons Chemical class 0.000 title description 4
- 239000004215 Carbon black (E152) Substances 0.000 title 1
- 229910052751 metal Inorganic materials 0.000 claims abstract description 14
- 239000002184 metal Substances 0.000 claims abstract description 14
- 229930195734 saturated hydrocarbon Natural products 0.000 claims abstract description 11
- 230000003197 catalytic effect Effects 0.000 abstract description 9
- 229920006395 saturated elastomer Polymers 0.000 abstract description 6
- 150000004945 aromatic hydrocarbons Chemical class 0.000 abstract description 5
- 238000006243 chemical reaction Methods 0.000 description 14
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 12
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 12
- YNQLUTRBYVCPMQ-UHFFFAOYSA-N Ethylbenzene Chemical compound CCC1=CC=CC=C1 YNQLUTRBYVCPMQ-UHFFFAOYSA-N 0.000 description 10
- 239000003054 catalyst Substances 0.000 description 7
- PPBRXRYQALVLMV-UHFFFAOYSA-N Styrene Chemical compound C=CC1=CC=CC=C1 PPBRXRYQALVLMV-UHFFFAOYSA-N 0.000 description 6
- 238000004227 thermal cracking Methods 0.000 description 4
- MYRTYDVEIRVNKP-UHFFFAOYSA-N 1,2-Divinylbenzene Chemical compound C=CC1=CC=CC=C1C=C MYRTYDVEIRVNKP-UHFFFAOYSA-N 0.000 description 2
- KVNYFPKFSJIPBJ-UHFFFAOYSA-N 1,2-diethylbenzene Chemical compound CCC1=CC=CC=C1CC KVNYFPKFSJIPBJ-UHFFFAOYSA-N 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- RWGFKTVRMDUZSP-UHFFFAOYSA-N cumene Chemical compound CC(C)C1=CC=CC=C1 RWGFKTVRMDUZSP-UHFFFAOYSA-N 0.000 description 2
- GNTDGMZSJNCJKK-UHFFFAOYSA-N divanadium pentaoxide Chemical compound O=[V](=O)O[V](=O)=O GNTDGMZSJNCJKK-UHFFFAOYSA-N 0.000 description 2
- 238000000034 method Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- HYFLWBNQFMXCPA-UHFFFAOYSA-N 1-ethyl-2-methylbenzene Chemical compound CCC1=CC=CC=C1C HYFLWBNQFMXCPA-UHFFFAOYSA-N 0.000 description 1
- 229910010413 TiO 2 Inorganic materials 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000000919 ceramic Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 229920003051 synthetic elastomer Polymers 0.000 description 1
- 239000005061 synthetic rubber Substances 0.000 description 1
- 229910052720 vanadium Inorganic materials 0.000 description 1
- LEONUFNNVUYDNQ-UHFFFAOYSA-N vanadium atom Chemical compound [V] LEONUFNNVUYDNQ-UHFFFAOYSA-N 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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- 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
- Y02P20/141—Feedstock
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- 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
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Abstract
本实用新型涉及一种反应器，提供了一种芳香饱和烃类催化反应脱氢反应器，包括圆形筒体、上封头、下封头、多孔外筒、多孔内筒、反应器进口、反应器出口和圆柱形金属体，上封头固定在筒体的上端，下封头固定在筒体的下端，多孔外筒设置在筒体内，多孔外筒与筒体之间的空隙为合流通道，多孔内筒设置在多孔外筒内，多孔内筒和多孔外筒与筒体共轴，多孔外筒和多孔内筒的底端与下封头密封连接，圆柱形金属体设置在多孔内筒内，其上端与多孔内筒相连接，反应器进口设置在下封头上，与多孔内筒相连通，反应器出口设置在上封头，与合流通道相连通。本实用新型可广泛的应用于饱和芳烃的催化脱氢反应，选择性可大于常规的反应器0.5～2％以上。
The utility model relates to a reactor, which provides a catalytic dehydrogenation reactor for aromatic saturated hydrocarbons, comprising a circular cylinder, an upper head, a lower head, a porous outer cylinder, a porous inner cylinder, a reactor inlet, The outlet of the reactor and the cylindrical metal body, the upper head is fixed on the upper end of the cylinder, the lower head is fixed on the lower end of the cylinder, the porous outer cylinder is set in the cylinder, and the gap between the porous outer cylinder and the cylinder is a confluence channel , the porous inner cylinder is arranged in the porous outer cylinder, the porous inner cylinder and the porous outer cylinder are coaxial with the cylinder body, the bottom ends of the porous outer cylinder and the porous inner cylinder are sealed and connected with the lower head, and the cylindrical metal body is arranged in the porous inner cylinder Inside, its upper end is connected with the porous inner cylinder, the reactor inlet is set on the lower head and communicates with the porous inner cylinder, and the reactor outlet is set on the upper head and communicates with the confluence channel. The utility model can be widely applied to the catalytic dehydrogenation reaction of saturated aromatic hydrocarbons, and the selectivity can be 0.5-2% higher than that of conventional reactors.
Description
技术领域 technical field
本实用新型涉及一种反应器，尤其涉及一种饱和芳烃的催化脱氢反应器。The utility model relates to a reactor, in particular to a catalytic dehydrogenation reactor for saturated aromatic hydrocarbons.
背景技术 Background technique
众所周知，饱和芳香烃都有一定的热化学稳定性，例如在高温下，比如大于600℃，不需要任何催化剂，甲苯就会侧链断裂生成苯和轻分子烃；在高温下，不需要任何催化剂，乙苯就会侧链断裂生成苯\甲苯\苯乙烯和轻分子烃；在高温下，不需要任何催化剂，甲乙苯\异丙苯\二乙苯等就会侧链断裂生成苯\甲苯\乙苯\苯乙烯\a甲基苯乙烯\乙烯基乙苯\二乙烯基苯和轻分子烃。As we all know, saturated aromatic hydrocarbons have certain thermochemical stability. For example, at high temperature, such as greater than 600 ° C, without any catalyst, toluene will break the side chain to generate benzene and light molecular hydrocarbons; at high temperature, no catalyst is needed. , ethylbenzene will break the side chain to generate benzene\toluene\styrene and light molecular hydrocarbons; at high temperature, without any catalyst, methylethylbenzene\isopropylbenzene\diethylbenzene will break the side chain to form benzene\toluene\ Ethylbenzene\styrene\amethylstyrene\vinylethylbenzene\divinylbenzene and light molecular hydrocarbons.
饱和芳烃的催化脱氢反应一般都是在较高的温度550-750℃下操作的，此时就会发生较显著的热裂解反应。例如刘中琦等(合成橡胶工业，1982，5(2)：109-116.)在接近工业的条件下，以不同的温度考察工业反应器和惰性填料上的空白转化，其中饱和烃乙苯进料速度为17克/小时，水蒸汽比为2.45，当温度从540℃升到640℃时，空白转化率从0.48％增加到4.07％，选择性在65％左右，如640℃下各产物的生成量分别为：苯0.56％，甲苯0.37％，苯乙烯3.15％，说明即使在不装催化剂的情况下，也有微量的乙苯转化，认为不锈钢反应器管壁对乙苯转化有一定的催化活性。The catalytic dehydrogenation reaction of saturated aromatics is generally operated at a relatively high temperature of 550-750°C, at which point a more significant thermal cracking reaction will occur. For example Liu Zhongqi etc. (synthetic rubber industry, 1982,5 (2): 109-116.) under the condition close to industry, investigate the blank conversion on industrial reactor and inert packing with different temperature, wherein saturated hydrocarbon ethylbenzene feedstock The speed is 17 g/h, the water vapor ratio is 2.45, when the temperature rises from 540°C to 640°C, the blank conversion rate increases from 0.48% to 4.07%, and the selectivity is around 65%, such as the formation of each product at 640°C The amounts are: 0.56% benzene, 0.37% toluene, and 3.15% styrene, indicating that even in the absence of a catalyst, there is a small amount of ethylbenzene conversion. It is believed that the stainless steel reactor tube wall has a certain catalytic activity for ethylbenzene conversion.
美国专利US 4132743也认为，高温下饱和芳烃与铁质反应器管壁直接接触，容易发生非选择性热裂解反应，裂解产物中目的产物含量较低，影响最终的反应选择性；同时指出：在反应器的内壁渡上一层含有惰性氧化物如五氧化二钒的薄膜，将会有效地抑制饱和烃热裂解；采用陶瓷反应器也可以降低热裂解程度；膜的成分应包括以下物质中的任一种或多种混合：Cr2O3，V2O5，TeO2，ZnO2，TiO2，钒金属及其硼化物。U.S. Patent No. 4132743 also believes that under high temperature, saturated aromatic hydrocarbons are in direct contact with the iron reactor tube wall, and non-selective thermal cracking reactions are prone to occur, and the content of the target product in the cracked products is low, which affects the final reaction selectivity; The inner wall of the reactor is covered with a film containing inert oxides such as vanadium pentoxide, which will effectively inhibit the thermal cracking of saturated hydrocarbons; the use of ceramic reactors can also reduce the degree of thermal cracking; the composition of the film should include the following substances Any one or mixture of more: Cr 2 O 3 , V 2 O 5 , TeO 2 , ZnO 2 , TiO 2 , vanadium metal and its borides.
所以一般会在此类装置中采用负压操作，从而降低饱和烃类在反应装置中的停留时间，提高此类装置的选择性。Therefore, negative pressure operation is generally used in such devices to reduce the residence time of saturated hydrocarbons in the reaction device and improve the selectivity of such devices.
美国专利US5358698和欧洲专利EP0724906A1描述了一种实施此类反应过程的环形催化床的装置和获得高效率反应过程的方法。中国专利ZL96114363.0中也描述了一种多维流动的反应装置实现负压低阻力的反应效果。U.S. Patent US5358698 and European Patent EP0724906A1 describe a device for implementing such a reaction process with an annular catalytic bed and a method for obtaining a high-efficiency reaction process. Chinese patent ZL96114363.0 also describes a multi-dimensional flow reaction device to realize the reaction effect of negative pressure and low resistance.
上述的专利所涉及的反应器，结构复杂，设备投资大，工业化实施有一定的难度。The reactors involved in the above-mentioned patents have complex structures, large investment in equipment, and certain difficulties in industrial implementation.
发明内容 Contents of the invention
本实用新型的目的是提供一种芳香饱和烃类催化反应脱氢反应器，以克服现有技术存在的缺陷，满足工业化生产的需要。The purpose of the utility model is to provide a catalytic dehydrogenation reactor for aromatic saturated hydrocarbons to overcome the defects of the prior art and meet the needs of industrial production.
本实用新型的芳香饱和烃类催化反应脱氢反应器，包括承受压力的圆形筒体、上封头、下封头、圆柱形多孔外筒、圆柱形多孔内筒、反应器进口、反应器出口和圆柱形金属体；The catalytic reaction dehydrogenation reactor for aromatic saturated hydrocarbons of the present utility model comprises a circular cylinder under pressure, an upper head, a lower head, a cylindrical porous outer cylinder, a cylindrical porous inner cylinder, a reactor inlet, and a reactor. Outlet and cylindrical metal body;
上封头固定在圆形筒体的上端，下封头固定在圆形筒体的下端，所述圆柱形多孔外筒设置在筒体内且与筒体共轴，圆柱形多孔外筒与筒体之间的空隙为合流通道，所述圆柱形多孔内筒设置在圆柱形多孔外筒内且与筒体共轴，圆柱形多孔外筒和圆柱形多孔内筒的底端与下封头密封连接，构成催化剂框，所述圆柱形金属体设置在圆柱形多孔内筒，其上端与圆柱形多孔内筒相连接，反应器进口设置在下封头上，与圆柱形多孔内筒相连通，反应器出口设置在上封头，与合流通道相连通。The upper head is fixed on the upper end of the circular cylinder, the lower head is fixed on the lower end of the circular cylinder, the cylindrical porous outer cylinder is arranged in the cylinder and coaxial with the cylinder, the cylindrical porous outer cylinder and the cylinder The gap between them is a confluence channel, the cylindrical porous inner cylinder is arranged in the cylindrical porous outer cylinder and is coaxial with the cylinder body, and the bottom ends of the cylindrical porous outer cylinder and the cylindrical porous inner cylinder are sealed and connected with the lower head , constituting the catalyst frame, the cylindrical metal body is arranged in the cylindrical porous inner cylinder, its upper end is connected with the cylindrical porous inner cylinder, the reactor inlet is arranged on the lower head, and communicates with the cylindrical porous inner cylinder, the reactor The outlet is set on the upper head and communicates with the confluence channel.
本实用新型是这样运行的：反应物流首先经反应器进口进入由圆柱形多孔内筒与圆柱形金属体之间的通道，而后通过圆柱形多孔内筒进入催化剂框，发生所须要的化学反应，反应后的流体通过圆柱形多孔外筒进入合流通道，然后通过反应器出口流出反应器。The utility model operates like this: the reactant flow first enters the channel between the cylindrical porous inner cylinder and the cylindrical metal body through the reactor inlet, and then enters the catalyst frame through the cylindrical porous inner cylinder, and the required chemical reaction occurs. The reacted fluid enters the confluence channel through the cylindrical porous outer cylinder, and then flows out of the reactor through the reactor outlet.
本实用新型的反应器，通过设置圆柱形金属体，降低了饱和烃类在进口通道中的停留时间，从而提高了反应过程的选择性，可广泛的应用于饱和芳烃的催化脱氢反应，选择性可大于常规的反应器0.5～2％以上。The reactor of the utility model reduces the residence time of saturated hydrocarbons in the inlet channel by setting a cylindrical metal body, thereby improving the selectivity of the reaction process, and can be widely used in the catalytic dehydrogenation reaction of saturated aromatic hydrocarbons. The resistance can be 0.5-2% greater than that of conventional reactors.
附图说明 Description of drawings
图1为反应器结构示意图。Figure 1 is a schematic diagram of the reactor structure.
具体实施方式 Detailed ways
参见图1，本实用新型的芳香饱和烃类催化反应脱氢反应器，包括承受压力的圆形筒体1、上封头2、下封头3、圆柱形多孔外筒4、圆柱形多孔内筒5、反应器进口7、反应器出口8和圆柱形金属体6；Referring to Fig. 1, the catalytic dehydrogenation reactor for aromatic saturated hydrocarbons of the present invention comprises a pressure-bearing
上封头2固定在圆形筒体1的上端，下封头3固定在圆形筒体1的下端，所述圆柱形多孔外筒4设置在筒体3内且与筒体3共轴，圆柱形多孔外筒4与筒体3之间的空隙为合流通道9，所述圆柱形多孔内筒5设置在圆柱形多孔外筒4内且与筒体3共轴，圆柱形多孔外筒4和圆柱形多孔内筒5的底端与下封头3密封连接，构成催化剂框10，所述圆柱形金属体6设置在圆柱形多孔内筒5，其上端与圆柱形多孔内筒5相连接，反应器进口7设置在下封头3上，与圆柱形多孔内筒5相连通，反应器出口8设置在上封头2，与合流通道9相连通。The
优选的，所述圆柱形金属体6的横截面面积为圆柱形多孔内筒5的横截面面积的20～95％，优选为60～95％。Preferably, the cross-sectional area of the
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102639227A (en) * | 2009-12-01 | 2012-08-15 | 巴斯夫欧洲公司 | Reactor for carrying out autothermal gas phase dehydrogenation |
| CN103958048A (en) * | 2011-08-02 | 2014-07-30 | 巴斯夫欧洲公司 | Continuous method for carrying out autothermal gas phase dehydrogenations |
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2008
- 2008-07-29 CN CNU2008201513828U patent/CN201276506Y/en not_active Expired - Lifetime
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102639227A (en) * | 2009-12-01 | 2012-08-15 | 巴斯夫欧洲公司 | Reactor for carrying out autothermal gas phase dehydrogenation |
| CN102639227B (en) * | 2009-12-01 | 2014-10-01 | 巴斯夫欧洲公司 | Reactor for carrying out autothermal gas phase dehydrogenation |
| CN103958048A (en) * | 2011-08-02 | 2014-07-30 | 巴斯夫欧洲公司 | Continuous method for carrying out autothermal gas phase dehydrogenations |
| CN103958048B (en) * | 2011-08-02 | 2016-11-16 | 巴斯夫欧洲公司 | For implementing the continuation method of autothermal gas-phase dehydrogenation |
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