JP2001157834A - Catalytic reactor having partition wall comprising porous membrane, method of manufacturing chemical substance using the same and reaction apparatus using reactor - Google Patents
Catalytic reactor having partition wall comprising porous membrane, method of manufacturing chemical substance using the same and reaction apparatus using reactorInfo
- Publication number
- JP2001157834A JP2001157834A JP34437899A JP34437899A JP2001157834A JP 2001157834 A JP2001157834 A JP 2001157834A JP 34437899 A JP34437899 A JP 34437899A JP 34437899 A JP34437899 A JP 34437899A JP 2001157834 A JP2001157834 A JP 2001157834A
- Authority
- JP
- Japan
- Prior art keywords
- reactor
- gas
- catalyst
- reaction
- reaction chamber
- 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.)
- Withdrawn
Links
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 76
- 239000012528 membrane Substances 0.000 title claims abstract description 22
- 230000003197 catalytic effect Effects 0.000 title claims abstract description 12
- 238000005192 partition Methods 0.000 title claims abstract description 8
- 239000000126 substance Substances 0.000 title claims description 13
- 238000004519 manufacturing process Methods 0.000 title claims description 7
- 239000003054 catalyst Substances 0.000 claims abstract description 28
- 238000000926 separation method Methods 0.000 claims description 11
- 238000000354 decomposition reaction Methods 0.000 claims description 9
- 239000002994 raw material Substances 0.000 claims description 7
- 238000001179 sorption measurement Methods 0.000 claims description 7
- 238000004821 distillation Methods 0.000 claims description 5
- 239000007789 gas Substances 0.000 description 44
- 239000000047 product Substances 0.000 description 8
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 6
- XDTMQSROBMDMFD-UHFFFAOYSA-N Cyclohexane Chemical compound C1CCCCC1 XDTMQSROBMDMFD-UHFFFAOYSA-N 0.000 description 5
- 230000000052 comparative effect Effects 0.000 description 5
- 238000006356 dehydrogenation reaction Methods 0.000 description 5
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 4
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 3
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- 239000001569 carbon dioxide Substances 0.000 description 3
- 229910002092 carbon dioxide Inorganic materials 0.000 description 3
- 229910001873 dinitrogen Inorganic materials 0.000 description 3
- 239000012466 permeate Substances 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 239000011261 inert gas Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000000034 method Methods 0.000 description 2
- 229910052697 platinum Inorganic materials 0.000 description 2
- -1 For example Substances 0.000 description 1
- 102100033040 Carbonic anhydrase 12 Human genes 0.000 description 1
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- 239000005977 Ethylene Substances 0.000 description 1
- 101000867855 Homo sapiens Carbonic anhydrase 12 Proteins 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 102100031083 Uteroglobin Human genes 0.000 description 1
- 108090000203 Uteroglobin Proteins 0.000 description 1
- 239000003463 adsorbent Substances 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000000919 ceramic Substances 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 239000007809 chemical reaction catalyst Substances 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 208000012839 conversion disease Diseases 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 238000007701 flash-distillation Methods 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000005295 porous vycor glass Substances 0.000 description 1
Classifications
-
- 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
- Separation Using Semi-Permeable Membranes (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Catalysts (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、新規な気体触媒反
応器及びそれを用いた化学物質の製造方法に関し、特
に、多孔膜からなる隔膜によって気体の流れ方向に沿っ
て２分された、気体分解反応用触媒反応器、及び、化学
平衡の移動を利用した化学物質の製造方法並びにこれら
の実用化のための反応装置に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a novel gas-catalyzed reactor and a method for producing a chemical substance using the same, and more particularly, to a method of dividing a gas into two by a porous membrane in the gas flow direction. The present invention relates to a catalytic reactor for a decomposition reaction, a method for producing a chemical substance using the transfer of chemical equilibrium, and a reaction apparatus for putting them into practical use.
【０００２】[0002]
【従来技術】平衡反応系において、物質透過性微細孔を
有する隔膜を介して該平衡反応系の物質を拡散除去する
ことにより平衡をずらし、平衡値を越える生成物を得る
ことのできる反応器、及び、隔膜を介し反応系から物質
が拡散してくる透過側に不活性ガスをスウィープガスと
して流すことにより、全体としての平衡値からのずれを
更に大きくすることができることは既に知られている
（ジャーナル オブ ケミカルエンジニアリング オブ
ジャパン、第２０巻、第４号、３９９頁〜４０４頁
（１９８８））。2. Description of the Related Art In an equilibrium reaction system, a reactor capable of shifting the equilibrium by diffusing and removing substances in the equilibrium reaction system through a membrane having material-permeable micropores to obtain a product exceeding the equilibrium value. It is already known that a deviation from an overall equilibrium value can be further increased by flowing an inert gas as a sweep gas to a permeation side where a substance diffuses from a reaction system through a diaphragm (see FIG. 1). Journal of Chemical Engineering of Japan, Vol. 20, No. 4, pp. 399-404 (1988)).
【０００３】このように、平衡反応における平衡転化率
によって制限される本来の生成量以上の生成物を得るこ
とは、生成物に対する需要が大きい場合ほど重要であ
る。例えば、エタンやシクロヘキサンの脱水素分解反応
における、エチレン、水素、ベンゼン等の需要は、エタ
ンやシクロヘキサン自身に対する需要よりも大きい。従
って、これらの分解反応を、平衡転化率以上に進めるこ
とが望まれるが、従来の方法による改善では未だ十分と
言えるものではなかった。[0003] As described above, it is more important to obtain a product whose amount is equal to or greater than the original production amount limited by the equilibrium conversion in the equilibrium reaction as the demand for the product is larger. For example, the demand for ethylene, hydrogen, benzene and the like in the dehydrogenation decomposition reaction of ethane and cyclohexane is larger than the demand for ethane and cyclohexane itself. Therefore, it is desired that these decomposition reactions proceed to an equilibrium conversion rate or higher, but improvement by the conventional method has not been sufficient.
【０００４】そこで本発明者らは、多孔膜を隔壁として
有する反応器を用い、平衡反応を更に大きくずらすこと
について鋭意検討した結果、スウィープガスを流す透過
側にも反応室に充填したものと同じ触媒を充填すること
により、従来より更に良好な結果を得ることができるこ
とを見出し本発明に到達した。[0004] The inventors of the present invention have used the reactor having the porous membrane as a partition wall, and have made intensive studies on further deviating the equilibrium reaction. It has been found that by filling the catalyst, better results can be obtained than before, and the present invention has been achieved.
【０００５】[0005]
【発明が解決しようとする課題】従って本発明の第１の
目的は、平衡反応の理論値を越える生成物を得るための
触媒反応器を提供することにある。本発明の第２の目的
は、平衡反応の理論値を越えて、より多くの有用な生成
物を得るための方法を提供することにある。更に本発明
の第３の目的は、平衡反応から得られる生成物を、理論
的平衡値を越えて効率良く得るための反応装置を提供す
ることにある。SUMMARY OF THE INVENTION It is therefore a first object of the present invention to provide a catalytic reactor for obtaining products which exceed the theoretical value of the equilibrium reaction. A second object of the present invention is to provide a method for obtaining more useful products beyond the theoretical value of the equilibrium reaction. A third object of the present invention is to provide a reactor for efficiently obtaining a product obtained from an equilibrium reaction exceeding a theoretical equilibrium value.
【０００６】[0006]
【課題を解決するための手段】本発明の上記の諸目的
は、ガス流入口とガス流出口を有し、内部に触媒を充填
してなる反応器であって、該反応器内部を２室に２分す
る如く、ガスの流れ方向に沿って物質透過性の多孔膜か
らなる隔壁が設けられてなる触媒反応器、及び、該反応
器を有する反応装置によって達成された。An object of the present invention is to provide a reactor having a gas inlet and a gas outlet and having a catalyst filled therein, wherein the inside of the reactor has two chambers. This was achieved by a catalytic reactor provided with a partition wall made of a porous material-permeable membrane along the gas flow direction, and a reactor having the reactor.
【０００７】[0007]
【発明の実施の形態】本発明の反応器は、夫々同一又は
同一種類の触媒が充填され、物質透過性の多孔膜によっ
て２室に分割された反応室からなると共に、一方の端部
に原料ガス又はスウィープガスを供給し得るガス供給
口、及び、他方の端部にガス排出口を有するものであれ
ば良く、その材質や形状等は公知のもののなかから適宜
選択することができる。また、上記多孔膜も、物質透過
性であって反応室壁を形成し得る公知のものの中から適
宜選択することができる。このような多孔膜としては、
例えば、多孔質バイコールガラスやセラミックス等を挙
げることができる。DESCRIPTION OF THE PREFERRED EMBODIMENTS The reactor of the present invention comprises a reaction chamber filled with the same or the same type of catalyst and divided into two chambers by a material-permeable porous membrane. Any material having a gas supply port capable of supplying gas or sweep gas and a gas discharge port at the other end may be used, and the material, shape, and the like can be appropriately selected from known ones. The porous membrane can also be appropriately selected from known substances which are permeable to substances and can form reaction chamber walls. As such a porous membrane,
For example, porous Vycor glass and ceramics can be used.
【０００８】本発明の反応器における第１、第２反応室
の２室のうち、第１反応室は原料ガスのみをガス供給口
から供給する主反応室であり、第２反応室はスウィープ
ガスのみをガス供給口から供給する副反応室である。該
副反応室には主反応室に充填した触媒と同一又は同種の
反応触媒が充填される。また、通常、主反応室には全域
にわたって触媒が充填されるが、副反応室には、ガス流
れ方向の後段部のみに充填することが好ましい。[0008] Of the first and second reaction chambers in the reactor of the present invention, the first reaction chamber is a main reaction chamber for supplying only a raw material gas from a gas supply port, and the second reaction chamber is a sweep gas. This is a sub-reaction chamber that supplies only gas from the gas supply port. The sub-reaction chamber is filled with the same or the same type of reaction catalyst as the catalyst charged in the main reaction chamber. Usually, the catalyst is filled in the entire main reaction chamber, but it is preferable that the sub-reaction chamber is filled only in the rear part in the gas flow direction.
【０００９】本発明の反応器が有効となる反応は、例え
ば、エタンやシクロヘキサンの脱水素分解反応等の化学
平衡の存在する触媒反応である。即ち、主反応室に原料
を供給すると平衡反応が生じ、多孔膜の透過膜がない場
合には、反応が平衡点に達した後は、見掛け上はそれ以
上反応が進むことはない。しかしながら、前記多孔膜を
通して原料ガスや生成ガスが拡散すると前記平衡が崩れ
ることになり、実際の反応は、理論上の平衡点を越えて
進行する。The reaction in which the reactor of the present invention is effective is, for example, a catalytic reaction having a chemical equilibrium such as a dehydrogenation decomposition reaction of ethane or cyclohexane. That is, when the raw material is supplied to the main reaction chamber, an equilibrium reaction occurs, and if there is no permeable membrane of the porous membrane, the reaction does not seem to proceed further after the reaction reaches the equilibrium point. However, when the source gas or the generated gas diffuses through the porous membrane, the equilibrium is broken, and the actual reaction proceeds beyond the theoretical equilibrium point.
【００１０】一方、副反応室には、多孔膜を通って主反
応室から透過してきたガスとスウィープガスが混在す
る。スウィープガスの一部は多孔膜を通って主反応室に
拡散する。従来は、副反応室におけるスウィープガス以
外のガスは、主反応室から透過してきた原料及び反応生
成物であり、これらの比率は、透過して来た量の比率で
ある。しかしながら、本発明においては副反応室にも触
媒を充填してあるので、透過してきた原料ガスが反応し
て、その分生成ガスの生成量が増大する。On the other hand, in the sub-reaction chamber, the gas permeated from the main reaction chamber through the porous membrane and the sweep gas are mixed. Some of the sweep gas diffuses through the porous membrane into the main reaction chamber. Conventionally, gases other than the sweep gas in the sub-reaction chamber are raw materials and reaction products that have permeated from the main reaction chamber, and their ratio is the ratio of the permeated amount. However, in the present invention, since the sub-reaction chamber is also filled with the catalyst, the permeated raw material gas reacts, and the amount of generated gas increases accordingly.
【００１１】反応転化率は副反応室の触媒の量にほぼ比
例するが、部分的に充填する場合には、ガス排出口から
順次手前に充填することが好ましい。スウィープガスは
非反応性のガスの中から適宜選択して使用することがで
きる。特に、窒素ガス及び炭酸ガスが安価であるので好
ましい。以下、本発明を図面に従って更に詳述する。Although the reaction conversion is substantially proportional to the amount of the catalyst in the sub-reaction chamber, when partially charged, it is preferable to sequentially fill the gas from the gas outlet. The sweep gas can be appropriately selected from non-reactive gases and used. In particular, nitrogen gas and carbon dioxide gas are preferable because they are inexpensive. Hereinafter, the present invention will be described in more detail with reference to the drawings.
【００１２】図１は、多孔膜を隔壁として有する、従来
の反応器を用いた、シクロヘキサンの脱水素分解反応系
の概念図である。尚、図中の網掛け部は触媒を有する反
応室、網掛けのない方は、原料や生成物が透過してくる
透過室であり、この透過室に触媒は存在しない。また、
透過室には不活性なスウィープガスを供給するが、スウ
ィープガスの１部は主反応室側に透過する。スウィープ
ガスは窒素ガス、炭酸ガス、希ガス等、公知の不活性な
ガスの中から適宜選択することができるが、経済性の観
点から、特に窒素ガス又は炭酸ガスが好ましい。FIG. 1 is a conceptual diagram of a cyclohexane dehydrogenation decomposition reaction system using a conventional reactor having a porous membrane as a partition. The shaded area in the figure is a reaction chamber having a catalyst, and the unshaded area is a permeation chamber through which raw materials and products permeate, and no catalyst is present in this permeation chamber. Also,
An inert sweep gas is supplied to the permeation chamber, and a part of the sweep gas permeates to the main reaction chamber. The sweep gas can be appropriately selected from known inert gases such as a nitrogen gas, a carbon dioxide gas, and a rare gas. From the viewpoint of economy, a nitrogen gas or a carbon dioxide gas is particularly preferable.
【００１３】図２は、多孔膜を隔壁として有する本発明
の反応器である。本図においては、原料ガスを供給する
主反応室、及び、スウィープスガスを供給する副反応室
の何れにも、同一の触媒が同じように充填されている
が、副反応室の触媒は部分的に充填されていても良い
（図３参照）。しかしながら、少なくとも、ガス流出口
近傍には充填されていることが好ましい。FIG. 2 shows a reactor of the present invention having a porous membrane as a partition. In this figure, the same catalyst is similarly filled in both the main reaction chamber for supplying the raw material gas and the sub-reaction chamber for supplying the sweep gas, but the catalyst in the sub-reaction chamber is partially filled. It may be filled (see FIG. 3). However, it is preferable that at least the vicinity of the gas outlet is filled.
【００１４】反応器の形状は特に限定されず、図２の如
く主反応室と副反応室が平面状の多孔膜によって単に仕
切られていても、主反応室と副反応室の関係が、芯と鞘
の関係のようになっていても良い。このような反応器と
することにより、後述する如く、全体としての反応率を
従来の場合より大幅に増大させることができるだけでな
く、スウィープスガスの使用量も特に多いという程でも
ないので、生成物の分離も容易である。The shape of the reactor is not particularly limited. Even if the main reaction chamber and the sub-reaction chamber are simply separated by a planar porous membrane as shown in FIG. It may be like a relationship between the sheath. By using such a reactor, as described later, not only can the overall reaction rate be significantly increased than in the conventional case, but the amount of sweep gas used is not particularly large, so Separation of objects is also easy.
【００１５】図４は本発明の反応器を有する本発明の反
応装置の概念図である。図中、符号Ｒは多孔膜隔壁を有
する本発明の反応器、Ａ１及びＡ２は吸着分離塔、Ｍ１
〜Ｍ ４は混合機、ＦＤはフラッシュ蒸留機、Ｄは蒸留分
離機である。吸着分離塔に充填する吸着剤は公知のもの
の中から適宜選択することができるが、通常は活性炭を
使用する。また、吸着分離塔の代りに圧縮器を用い、圧
縮して液化するものと液化しないものに分離しても良
い。蒸留分離塔も公知のものの中から適宜選択すること
ができる。FIG. 4 shows the reaction of the present invention having the reactor of the present invention.
It is a conceptual diagram of a response apparatus. In the figure, the symbol R has a porous membrane partition.
A of the present invention,1And A2Is the adsorption separation column, M1
~ M 4Is a blender, FD is a flash still, D is a distillation fraction
It is a takeoff machine. Known adsorbents to be packed in the adsorption separation tower
Can be selected as appropriate, but usually activated carbon is
use. In addition, a compressor is used instead of the adsorption
It can be separated into those that liquefy and those that do not liquefy
No. The distillation separation column should also be appropriately selected from known ones.
Can be.
【００１６】[0016]
【発明の効果】本発明の触媒反応器を用いれば、単に化
学平衡を崩すだけでなく、透過膜通過後にも反応が進行
するので、全体として、化学平衡を大きく越えた量の生
成物を得ることができる。従って分解反応によってクリ
ーンエネルギー源として使用し得る水素ガスを製造する
場合に、本発明は特に有効である。以下、本発明を実施
例によって更に詳述するが、本発明はこれによって限定
されるものではない。According to the catalytic reactor of the present invention, not only the chemical equilibrium is destroyed, but also the reaction proceeds after passing through the permeable membrane, so that the amount of the product greatly exceeds the chemical equilibrium as a whole. be able to. Therefore, the present invention is particularly effective when producing hydrogen gas that can be used as a clean energy source by a decomposition reaction. Hereinafter, the present invention will be described in more detail by way of examples, but the present invention is not limited thereto.
【００１７】実施例１．図２の本発明の反応器を用いて
エタンの脱水素分解反応Ｃ２Ｈ６＝Ｃ２Ｈ４＋Ｈ２を行
った。触媒としては顆粒状の白金触媒を用い、１気圧、
７００℃で主反応室におけるガス空間速度を４．０６ｃ
ｍ３ＳＴＰ／分（これをＦとする）として実験を行っ
た。この結果、本発明の反応器を用いた場合には、主反
応室出口における各ガスの検出量は[Ｃ２Ｈ６]＝０．１
２４Ｆ、[Ｃ２Ｈ４]＝０．２９７Ｆ、[Ｈ２]＝０．１１
６Ｆ、[Ｎ２]＝０．７４４Ｆであり、副反応室出口にお
いては、[Ｃ２Ｈ６]＝０．２３１Ｆ、[Ｃ２Ｈ４]＝０．
３４８Ｆ、[Ｈ２]＝０．５３５Ｆ、[Ｎ２]＝８．２５６
Ｆであった。また、全転化率は６４．５％であった。Embodiment 1 FIG. The ethane dehydrogenation decomposition reaction C 2 H 6 ＣC 2 H 4 + H 2 was carried out using the reactor of the present invention shown in FIG. As a catalyst, a granular platinum catalyst was used, and the pressure was 1 atm.
At 700 ° C., the gas space velocity in the main reaction chamber is 4.06 c.
The experiment was performed with m 3 STP / min (this is F). As a result, when the reactor of the present invention was used, the detected amount of each gas at the outlet of the main reaction chamber was [C 2 H 6 ] = 0.1
24F, [C 2 H 4] = 0.297F, [H 2] = 0.11
6F, [N 2 ] = 0.744F, and [C 2 H 6 ] = 0.231F, [C 2 H 4 ] = 0.
348F, [H 2] = 0.535F , [N 2] = 8.256
F. The total conversion was 64.5%.
【００１８】比較例１．図２の本発明の反応器の代り
に、従来型である図１の反応器を用いた他は実施例１と
全く同様にしたところ、反応室出口における各ガスの検
出量は、[Ｃ２Ｈ ６]＝０．１２４Ｆ、[Ｃ２Ｈ４]＝０．
２９８Ｆ、[Ｈ２]＝０．１０９Ｆ、[Ｎ２]＝０．７４５
Ｆであり、透過室出口においては、[Ｃ２Ｈ６]＝０．２
６３Ｆ、[Ｃ２Ｈ４]＝０．３１６Ｆ、[Ｈ２]＝０．５０
５Ｆ、[Ｎ２]＝８．２５５Ｆであった。また、全反応量
は６１．４％であった。実施例１及び比較例１から明ら
かなように、本発明の反応器を用いることにより、全体
の反応率を増大させることのできることが実証された。Comparative Example 1 Instead of the reactor of the invention of FIG.
Example 1 was the same as Example 1 except that the conventional reactor of FIG. 1 was used.
When exactly the same was done, the detection of each gas at the reaction chamber outlet was performed.
The output is [C2H 6] = 0.124F, [C2H4] = 0.
298F, [H2] = 0.109F, [N2] = 0.745
F, and at the exit of the permeation chamber, [C2H6] = 0.2
63F, [C2H4] = 0.316F, [H2] = 0.50
5F, [N2] = 8.255F. Also, the total reaction volume
Was 61.4%. It is clear from Example 1 and Comparative Example 1.
As you can see, by using the reactor of the present invention,
Has been demonstrated to be able to increase the reaction rate.
【００１９】実施例２．図２の本発明の反応器（ＭＰＭ
Ｒ）を用いてシクロヘクサンの脱水素分解反応Ｃ６Ｈ
１２＝Ｃ６Ｈ６＋３Ｈ２を、１気圧、１８０℃の条件で
行った。触媒としては顆粒状の白金を用い、主反応室に
おけるガス空間速度を３５−１００ｃｍ３ＳＴＰ／分
（Ｄａ換算で１．９２−０．７２）、スウェープガス
（Ｎ２）速度を２５０ｃｍ３ＳＴＰ／分とした。Ｄａは
反応による生成速度を供給速度で除したものである。結
果は図５に示した通りである。Embodiment 2 FIG. The reactor (MPM) of the present invention shown in FIG.
R), the dehydrogenation decomposition reaction of cyclohexane C 6 H
12 = C 6 H 6 + 3H 2 was performed under the conditions of 1 atm and 180 ° C. As the catalyst used granular platinum, 35-100cm 3 STP / min of gas space velocity in the main reaction chamber (in Da terms 1.92-0.72), Suwepugasu the (N 2) speed 250 cm 3 STP / min And Da is a value obtained by dividing the production rate by the reaction by the supply rate. The results are as shown in FIG.
【００２０】比較例２．反応器として、図１の従来の反
応器（ＣＰＭＲ）を用いた他は実施例２と全く同様にし
て反応を行わせた。結果は、図５に示した通りである。
実施例２の結果と比較例２の結果から、図２の本発明の
反応器を用いた場合には図１の従来の反応器（ＣＰＭ
Ｒ）を用いた場合より優れた結果を得ることのできるこ
とが実証された。また、Ｄａ＝１．９２では、ＣＰＭＲ
の全転化率は３．７５％、実施例２の全転化率は５．５
０％であり、比較例２の場合より４７％増大しているこ
とが確認された。Comparative Example 2 The reaction was carried out in exactly the same manner as in Example 2 except that the conventional reactor (CPMR) shown in FIG. 1 was used as the reactor. The results are as shown in FIG.
From the results of Example 2 and Comparative Example 2, when the reactor of the present invention of FIG. 2 was used, the conventional reactor (CPM) of FIG. 1 was used.
It was demonstrated that superior results could be obtained with R). Also, when Da = 1.92, the CPMR
Is 3.75%, and the total conversion of Example 2 is 5.5.
0%, which was confirmed to be 47% higher than that of Comparative Example 2.
【００２１】実施例３．本発明の反応器を用いてＣ６Ｈ
１２＝Ｃ６Ｈ６＋３Ｈ２の反応を行い、副反応室の触媒
充填率に対する全転化率依存性を調べた。結果は図６に
示した通りである。この結果は、触媒の充填率がゼロの
従来の反応器より、透過側に触媒を充填した本発明の反
応器の場合の方が全転化率が大きいこと、即ち、副反応
室に触媒を充填することによって転化率が改善されるこ
とを実証するものである。Embodiment 3 FIG. C 6 H using the reactor of the present invention
A reaction of 12 = C 6 H 6 + 3H 2 was performed, and the dependence of the total conversion on the catalyst loading in the sub-reaction chamber was examined. The results are as shown in FIG. This result indicates that the total conversion is higher in the case of the reactor of the present invention in which the permeate side is filled with the catalyst than in the case of the conventional reactor in which the catalyst fill rate is zero, that is, the auxiliary reaction chamber is filled with the catalyst. This demonstrates that conversion improves the conversion.
【図１】多孔膜を用いた従来の反応器である。FIG. 1 shows a conventional reactor using a porous membrane.
【図２】多孔膜を用いた本発明の反応器である。FIG. 2 shows a reactor of the present invention using a porous membrane.
【図３】本発明の反応器における副反応室の触媒充填状
態を変えた場合を説明する図である。FIG. 3 is a diagram illustrating a case where the state of filling a catalyst in a sub-reaction chamber in the reactor of the present invention is changed.
【図４】本発明の反応装置の概念図である。FIG. 4 is a conceptual diagram of the reaction apparatus of the present invention.
【図５】本発明の反応器と従来の反応器における全転化
率のＤａ依存性を表すグラフである。FIG. 5 is a graph showing the Da dependence of the total conversion in the reactor of the present invention and the conventional reactor.
【図６】全転化率の、副反応室の触媒充填量に対する依
存性を表すグラフである。FIG. 6 is a graph showing the dependence of the total conversion on the catalyst loading in the sub-reaction chamber.
Ｒ 本発明の反応器 Ａ１ 吸着分離塔 Ａ２ 吸着分離塔 Ｍ１ 混合機 Ｍ２ 混合機 Ｍ３ 混合機 Ｍ４ 混合機 ＦＤ フラッシュ蒸留機 Ｄ 蒸留分離機R Reactor of the present invention A 1 adsorption separation tower A 2 adsorption separation tower M 1 mixer M 2 mixer M 3 mixer M 4 mixer FD flash distillation machine D distillation separation machine
フロントページの続き (51)Int.Cl.7 識別記号 ＦＩ テーマコート゛(参考） Ｃ０７Ｃ 11/04 Ｃ０７Ｃ 11/04 // Ｃ０７Ｂ 61/00 ３００ Ｃ０７Ｂ 61/00 ３００ Ｆターム(参考） 4D006 GA41 KB30 MA02 MA03 MC03 MC04 PB20 PB66 PC80 4G069 AA08 AA15 BC75B CB07 CB11 CB12 EA02Y FB77 4G070 AA01 AB02 BB05 CA01 CA12 CB15 4H006 AA02 AA04 AC12 BA26 BD35 BD52 BD81 4H039 CA21 CA41 CC10 Continued on the front page (51) Int.Cl. 7 Identification symbol FI Theme coat II (reference) C07C 11/04 C07C 11/04 // C07B 61/00 300 C07B 61/00 300 F term (reference) 4D006 GA41 KB30 MA02 MA03 MC03 MC04 PB20 PB66 PC80 4G069 AA08 AA15 BC75B CB07 CB11 CB12 EA02Y FB77 4G070 AA01 AB02 BB05 CA01 CA12 CB15 4H006 AA02 AA04 AC12 BA26 BD35 BD52 BD81 4H039 CA21 CA41 CC10
Claims (5)
触媒を充填してなる反応器であって、該反応器内部を２
室に２分する如く、ガスの流れ方向に沿って物質透過性
の多孔膜からなる隔壁が設けられてなる触媒反応器。1. A reactor having a gas inlet and a gas outlet and having a catalyst filled therein.
A catalytic reactor in which a partition made of a material-permeable porous membrane is provided along the gas flow direction so as to be divided into two chambers.
ガスの流れ方向に対して部分的に充填されていることを
特徴とする、請求項１に記載された触媒反応器。2. The catalyst in one of the reaction chambers,
2. The catalytic reactor according to claim 1, wherein the catalytic reactor is partially filled in the gas flow direction.
ガスの流出口近傍のみに充填されていることを特徴とす
る、請求項１に記載された触媒反応器。3. The catalyst in one of the reaction chambers,
2. The catalytic reactor according to claim 1, wherein the catalyst is filled only in the vicinity of the gas outlet.
反応器における、一方の第１反応室に分解反応用触媒が
充填され、他方の第２反応室には、中央よりガス出口側
の部分に同じ触媒が充填されている反応器の、前記第１
反応室側のガス流入口から原料ガスを供給し、第２反応
室側のガス流入口からは非反応性のスウィープガスを供
給することを特徴とする、化学物質の製造方法。4. The catalyst reactor according to claim 1, wherein one of the first reaction chambers is filled with a catalyst for a decomposition reaction, and the other second reaction chamber has a gas outlet from the center. The first part of the reactor, the side part of which is filled with the same catalyst,
A method for producing a chemical substance, comprising supplying a raw material gas from a gas inlet on a reaction chamber side and supplying a non-reactive sweep gas from a gas inlet on a second reaction chamber side.
反応器、及び吸着分離塔並びに蒸留分離塔を有する反応
装置であって、請求項４の製造方法によって製造した化
学物質を分取すると共に、非反応性のスウィープガスを
リサイクルする如く、前記反応器、吸着分離塔及び蒸留
分離塔を連結して成ることを特徴とする反応装置。5. A reactor having the catalytic reactor according to claim 1, an adsorption separation column and a distillation separation column, wherein the chemical substance produced by the production method according to claim 4 is separated. A reaction apparatus, wherein the reactor, the adsorption separation tower, and the distillation separation tower are connected so as to recycle the non-reactive sweep gas.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP34437899A JP2001157834A (en) | 1999-12-03 | 1999-12-03 | Catalytic reactor having partition wall comprising porous membrane, method of manufacturing chemical substance using the same and reaction apparatus using reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP34437899A JP2001157834A (en) | 1999-12-03 | 1999-12-03 | Catalytic reactor having partition wall comprising porous membrane, method of manufacturing chemical substance using the same and reaction apparatus using reactor |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JP2001157834A true JP2001157834A (en) | 2001-06-12 |
Family
ID=18368790
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP34437899A Withdrawn JP2001157834A (en) | 1999-12-03 | 1999-12-03 | Catalytic reactor having partition wall comprising porous membrane, method of manufacturing chemical substance using the same and reaction apparatus using reactor |
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| Country | Link |
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| JP (1) | JP2001157834A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US9745191B2 (en) | 2011-04-11 | 2017-08-29 | Saudi Arabian Oil Company | Auto thermal reforming (ATR) catalytic structures |
-
1999
- 1999-12-03 JP JP34437899A patent/JP2001157834A/en not_active Withdrawn
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US9745191B2 (en) | 2011-04-11 | 2017-08-29 | Saudi Arabian Oil Company | Auto thermal reforming (ATR) catalytic structures |
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