CN100509720C - Reacting system and method for preparing styrene by negative pressure ethylbenzene catalytic dehydrogenation - Google Patents
Reacting system and method for preparing styrene by negative pressure ethylbenzene catalytic dehydrogenation Download PDFInfo
- Publication number
- CN100509720C CN100509720C CNB2005100231613A CN200510023161A CN100509720C CN 100509720 C CN100509720 C CN 100509720C CN B2005100231613 A CNB2005100231613 A CN B2005100231613A CN 200510023161 A CN200510023161 A CN 200510023161A CN 100509720 C CN100509720 C CN 100509720C
- Authority
- CN
- China
- Prior art keywords
- reactor
- type radial
- negative pressure
- ethylbenzene
- reactive system
- 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.)
- Active
Links
Images
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
A fixing bed radial reacting system for preparing phenylethylene by negative pressure ethylbenzene catalytic dehydrogenation and its method are disclosed. The reacting system consists of pai type radial reactor and Z type radial reactor combination, or pai type radial reactor and pai type radial reactor combination. Its advantages include low pressure drop, short gas stopping time, high efficiency and simple structure.
Description
Technical field
The invention belongs to the hydro carbons processing technique field, relate to a kind of fixed bed that is applicable to preparing styrene by negative pressure ethylbenzene catalytic dehydrogenation radially reactive system and method.
Background technology
Vinylbenzene is widely used as production various kinds of resin, plastics and elastomeric raw material, extensively mainly being easy to polymerization (for example generating polystyrene) owing to vinylbenzene or carrying out the adaptability of copolymerization (for example producing rubber with butadiene copolymer) of its range of application.
The preparing phenylethylene from dehydrogenation of phenylethane method is the topmost method of vinylbenzene of producing, and 90% vinylbenzene is produced by this method in the world.The technological principle of preparing phenylethylene from dehydrogenation of phenylethane is, ethylbenzene and water vapour are under the catalyzer existence condition, and under 500～650 ℃ of high temperature, ethylbenzene generation dehydrogenation reaction generates vinylbenzene, the feature of reaction be reversible, absorb heat, increase molecular reaction.Therefore, the method of preparing phenylethylene from dehydrogenation of phenylethane all adopts negative pressure technology (reacting system pressure is 70～30kPaA) in the current industrial, and adopt a large amount of water vapour as thermophore and thinner, the volume ratio of water vapour and ethylbenzene is up to 6～10, so the pressure-losses of reactive system is very big to the system response Effect on Performance, usually system pressure is lost in about 15～30kPa, so Ethylbenzene Dehydrogenation Reactor all adopts the radial reactor of low pressure drop.
The production of preparing phenylethylene from dehydrogenation of phenylethane with regard to the used various catalyzer of dehydrogenating technology and dehydrogenation reaction, is all known.Main goal in research is to improve the benefit of this reactive system and method at present.The dehydrogenating technology method of known ethylbenzene particularly, wherein dehydrogenation reaction be a cover comprise two placed in-line dehydrogenation reactors at least and place between the reactor, reaction effluent and vapor generation heat exchange therein and heated heating unit carries out.
The Production Flow Chart of common preparing phenylethylene from dehydrogenation of phenylethane has two kinds in the industry.A kind of flow process as shown in Figure 1, after ethylbenzene and high-temperature vapor mix in mixing tank, enter reactor central tube from first reactor bottom, under the control of baffle, fluid is radially by the annular beds, enter the annular outer flow passage, flow from bottom to top and flow out from reactor head, after after reheater improves temperature, enter reactor central tube from the top of second reactor, under the control of baffle, fluid is radially by the annular beds, enter the annular outer flow passage, flow from top to bottom and flow out, enter horizontally disposed combination exchanger subsequently and reclaim heat from the reactor-side basifacial.Another kind of flow process is shown in 2, after ethylbenzene and high-temperature vapor mix in mixing tank, enter reactor central tube from first reactor bottom, under the control of baffle, fluid is radially evenly by the annular beds, enter the annular outer flow passage, flow from bottom to top and flow out from reactor head, after after reheater improves temperature, enter reactor central tube from the end of second reactor, by the uniform effect of baffle, fluid is radially by the annular beds, enter the annular outer flow passage, flow from bottom to top and flow out, enter vertical combination exchanger subsequently and reclaim heat from reactor head.First reactor in the flow process and second reactor are the axial-radial flow reactor that there is the radial reactor of cover plate at the catalytic bed top or does not have cover plate, all adopted from bottom to top or Z type liquid form from top to bottom, combination exchanger is three vertically disposed unitized constructions.
Investigate aforementioned production method and structure of reactor, there are the following problems:
1, flow process shown in Figure 1, pipeline connects compact, but the combination exchanger that reclaims reactor discharging sensible heat adopts linear combination structure level direction to be provided with, and floor space is big, and because the deadweight of heat transfer tube is subjected to the direction of force direction and thermal expansion to be mutually 90 degree, the irrationality of this structure, make combination exchanger very easily produce leakage, heat is big in addition, and the temperature drop that hot-fluid is imported and exported is up to more than 200 ℃, thermal expansion amount is big, when serious even can draw bad heat transfer tube.Because of the leakage of interchanger, influence the normal running of reaction unit in the production process, caused the efficient of reactive system to descend significantly;
2, flow process shown in Figure 2 adopts the U-shaped pipeline to connect between second reactor and the reheater, make connection line extend, the residence time increases, cause thermo-cracking under the high temperature, side reaction increases, and bend pipe is many in addition, the reactive system pressure drop increases, calorific loss increases, and this and response feature are that technology reversible, that absorb heat, increase molecular reaction is runed counter to, though there is not the leakage problem of interchanger, but unreasonable because of reactive system makes that also the reactivity worth of system is not good enough;
3, propose a kind of high temperature sensible heat among document CN2557914Y and the CN1140161A and reclaimed unitized exchanger (Fig. 3), mainly solving heat-exchange equipment independently places separately, floor space is big, the pipe connecting line length, the pipeline droop loss is big, the problem that the pipeline calorific loss is big, but in the reactive system flow process of the dehydrogenation of ethylbenzene to styrene of its proposition, first and second reactors are down the Z type radial reactor that outes; Caused the connection that is provided with three U-shaped pipelines in the reactive system thus, thus identical with Fig. 2, can further increase systemic resistance, the residence time also increases, and is unfavorable to the ethylbenzene catalytic dehydrogenation reaction, makes the reactivity worth of system descend.
4, a kind of catalytic reforming and catalytic dehydrogenation fixed bed radial reactor are disclosed among the document CN1546217A, it is characterized by the same end that gas feed and pneumatic outlet are positioned at reactor, it is even vertically to have reactant gases, in catalytic bed, make pure radial flow, characteristics such as the pressure drop of the reactor of flowing through is little.But its porous wall inner core adopts and becomes percentage of open area or become diameter technology, complex structure; The porous wall percentage of open area is lower, has sizable pressure drop, generally is applicable to the compressive reaction system.But native system is the reaction process of the ethyl benzene dehydrogenation preparation of styrene under vacuum condition, and the reactor of its use is preferably low pressure drop or minute-pressure is fallen, and any structure of reactor that increases pressure drop slightly will be subjected to strict restriction in system.
Summary of the invention
The technical issues that need to address of the present invention are:
(1) by the appropriate design of reactor runner, adopt the porous wall structure of large opening rate, make reactor pressure decrease descend greatly;
(2) by the appropriate design of structure of reactor, cancel the baffle inner member in the reactor, reduce the manufacturing and the installation difficulty of reactor;
(3), get so that being evenly distributed of reactant gases guaranteed the raising of catalyst utilization by the radial reactor structure optimization design;
(4) provide the reaction method of the negative pressure catalytic dehydrogenation of a kind of low pressure drop and short residence time(SRT), guarantee that connection between each device is the most reasonable and optimize;
(5) by the combination of Π type radial reactor and Π type radial reactor or Z type radial reactor, satisfy the requirement of different pipe arrangements in the technical process, reactive system efficient is improved.
The present invention solves the problems of the technologies described above with this by the radially multiple array mode between negative pressure catalytic dehydrogenating reaction device and Π type and the Z type radial reactor of a kind of Π type is provided, and overcomes the defective that exists in the prior art; Developed simultaneously and met the ethylbenzene dehydrogenation reaction requirement fully, had low pressure drop, the very uniform Π type of gas distribution radial reactor.
According to above-mentioned design, the present invention proposes technical scheme as described below:
A kind of ethylbenzene catalytic dehydrogenation reactive system, comprise at least two catalytic dehydrogenating reaction devices, it is characterized in that, described ethylbenzene catalytic dehydrogenation reactive system adopts Π type radial reactor and the combination of Z type radial reactor, or Π type radial reactor and Π type radial reactor combine, and wherein has resuperheater to be connected between the outlet and second Reactor inlet of first reactor.
The Π type radial reactor that ethylbenzene negative pressure catalytic dehydrogenation preparation of styrene reactive system is adopted, comprise catalytic bed (5) in a cylindrical vessel (8) and the container, on the top of cylindrical vessel (8) or the same end of bottom reacting gas inlet (1) and reaction gas outlet (2) are set, on cylindrical vessel (8), are provided with catalyzer discharge tube (11); In cylindrical vessel (8), comprise: with the coaxial setting of cylindrical vessel (8), arrange porous wall inner core (6) and porous wall urceolus (7) from inside to outside according to this, porous wall inner core (6) is connected with reacting gas inlet (1), constitute the flow manifold (3) of reactant gases, form annular catalytic bed (5) between porous wall inner core (6) and the porous wall urceolus (7), constitute reactant gases afflux runner (4) between porous wall urceolus (7) and the cylindrical vessel (8), and be connected with reaction gas outlet (2); It is characterized in that the flow direction of reactant gases in afflux runner and flow manifold is opposite, the area ratio of flow manifold and afflux runner is 0.28～2.2, and the catalyst layer top can have cover plate also can not have cover plate.
The method that the present invention also provides a kind of ethylbenzene negative pressure catalytic dehydrogenation preparation of styrene reactive system to be adopted: the mixed material of ethylbenzene material and high-temperature vapor enters first reactor, behind the beds internal reaction, flow out from first reactor outlet, after promoting temperature, resuperheater enters second reactor, behind the beds internal reaction, flow out, enter interchanger and carry out heat recuperation from second reactor outlet.
Useful effect: the catalytic dehydrogenating reaction system adopts the combination process of Π type radial reactor and Π type radial reactor or Z type radial reactor, it is short all to have connection line, structure of reactor is simple, the characteristics that reactivity worth is good, and the difference of the import and export position of reactive system can satisfy the requirement of whole process system to reactor pipe arrangement position fully.It is little to have the total system pressure drop, and gas residence time is short, adapts to the negative dehydrogenation reaction characteristics under the vacuum condition, the adaptable characteristics of array mode of reactive system efficient height, reactive system.
In the Π type radial reactor, the area ratio of flow manifold and afflux runner is 0.28～2.2 o'clock, can cancel the setting of center baffle, has simplified the structure and the installation difficulty of reactor; Adopt the porous wall of large opening rate, reduce the perforation pressure drop.Catalyst layer top in the Π type radial reactor can have cover plate also can not have cover plate, and when adding cover plate, reactor is a radial flow reactors; When no cover plate, reactor is an axial-radial flow reactor, and reaction mass is a radial flow in the bed main body, and flowing in catalyst sealing is that the diameter of axle flows to two dimension.
Adopt above-mentioned Π type radial reactor, reactant gases is even along the bed axial distribution, the catalyst utilization height, and side reaction reduces, and structure of reactor is simple, and manufacture difficulty reduces.
Description of drawings
Fig. 1 ethyl benzene dehydrogenation preparation of styrene industrial flow 1;
Fig. 2 ethyl benzene dehydrogenation preparation of styrene industrial flow 2;
Fig. 3 high temperature sensible heat reclaims unitized exchanger and flow process;
Fig. 4 is of the present invention to go out radially catalytic dehydrogenating reaction device structural representation of Π type fixed bed on enterprising;
Wherein: 1-reacting gas inlet; 2-reaction gas outlet; 3-reactant gases flow manifold; 4-reactant gases afflux runner; 5-catalytic bed; 6-porous wall inner core; 7-porous wall urceolus; 8-cylindrical vessel; 9-inert particle material; 10-catalyst sealing; 11-catalyzer discharge tube;
Go out radially catalytic dehydrogenating reaction device structural representation of Π type fixed bed under advancing under Fig. 5 is of the present invention
Wherein: 1-reacting gas inlet; 2-reaction gas outlet; 3-reactant gases flow manifold; 4-reactant gases afflux runner; 5-catalytic bed; 6-porous wall inner core; 7-porous wall urceolus; 8-cylindrical vessel; 9-inert particle material; 10-catalyst sealing; 11-catalyzer discharge tube;
Fig. 6 Z type of the present invention (going out on advancing down) and Π type (going out on enterprising) radial reactor combination process.
Fig. 7 Z type of the present invention (going out under enterprising) and Π type (going out under advancing down) radial reactor combination process.
Fig. 8 Π type of the present invention (going out under advancing down) and Z type (going out on advancing down) radial reactor combination process.
Fig. 9 Π type of the present invention (going out on enterprising) and Π type (going out on enterprising) radial reactor combination process.
Figure 10 Π type of the present invention (going out under advancing down) and Π type (going out under advancing down) radial reactor combination process.
Embodiment
The present invention is further illustrated below in conjunction with the drawings and the specific embodiments, and institute's accompanying drawing of painting just helps to understand the present invention, and it does not limit protection scope of the present invention:
As seen from Figure 4, the present invention said go out on enterprising the Π type radially the catalytic dehydrogenating reaction device comprise:
In cylindrical vessel 8, comprise: with cylindrical vessel 8 coaxial settings, arrange not perforate of upper portion side wall, bottom perforate from inside to outside according to this and highly be the porous wall inner core 6 of H and whole urceolus 7 of the vesicular structure of perforates;
Described inner core 6 is connected with placing cylindrical vessel 8 top reacting gas inlets 1, constitute the flow manifold 3 of reactant gases, form catalytic bed 5 between inner core 6 and the urceolus 7, form reactant gases afflux runner 4 between porous wall urceolus and cylindrical vessel 8 sidewalls, reactant gases afflux runner 4 is connected with the reaction gas outlet 2 that places cylindrical vessel 8 upper side, and the cross-sectional area of reactant gases flow manifold 3 is advisable with 0.28～2.2 with the ratio of the cross-sectional area of reaction aerogenesis body afflux runner 4;
Described catalytic bed 5 tops are provided with one section inert particle material 9 and catalyst sealing 10, the height Δ H of catalyst sealing 10 is 0.2～5 times of bed radial thickness, the thickness of inert particle material 9 is 0.1～0.5 times of bed radial thickness, guarantees the diameter of axle the making full use of to mobile and catalyst sealing of reactant gases.
Since the invention process reactant gases reverse relative mobile structure in flow manifold 3 and afflux runner 4, interior porous wall tube 6 as the reactant gases sparger can keep sizable percentage of open area, the control pressure drop of reactant gases sparger can be ignored, when realizing not having the control pressure drop, guaranteed reactant gases uniform distribution vertically.
Structure and Fig. 1 of Fig. 5 are basic identical, but gas inlet tube 1 places on the bottom head of cylindrical vessel 8, and the outlet pipe 2 of reactant gases places the side bottom of cylindrical vessel 8.
Fig. 6 is Z type (going out on advancing down) and Π type (going out on enterprising) radial reactor combination process.First reactor is a Z type radial reactor, comprise catalytic bed in a cylindrical vessel and the container, the inboard flow manifold that forms of catalytic bed, inside comprises the taper baffle, the catalytic bed outside forms the afflux runner with the cylindrical vessel wall, and the import of reactor is in the bottom of flow manifold, and reactor outlet is at the top of afflux runner, the import and export of reactor lay respectively at the two ends of reactor, so be called Z type radial reactor.Reaction mass enters through first reactor lower part, behind the beds internal reaction, flow out from first reactor head, promote temperature through resuperheater, the top by second reactor enters reactor then, flows out from the second reactor head sidewall behind the beds internal reaction.The catalytic dehydrogenating reaction system adopts the array configuration of Z type radial reactor and Π type radial reactor, the Z type radial reactor of first reactor for going out on advancing down, second reactor is the Π type radial reactor that goes out on enterprising, between first reactor and second reactor resuperheater is arranged, as shown in Figure 6.It is short that this reaction process has connection line, structure of reactor is simple, the characteristics that reactive system efficient is high, and the second reactor outlet position can be satisfied follow-up interchanger fully and be adopted structures such as L shaped combination exchanger or the box-like interchanger of orthogonal sets, reduce the leakage of interchanger, improve negative pressure system efficient, reduce occupation area of equipment
Fig. 7 is Z type (going out under enterprising) and Π type (going out under advancing down) radial reactor combination process.Compare with Fig. 6, first Reactor inlet is reactor top, exports to be reactor bottom; The import of second reactor is a reactor bottom, exports to be the sidewall bottom.
Embodiment
Ethylbenzene negative pressure catalytic dehydrogenation preparation of styrene reactive system of the present invention can carry out in the flow process in office in the following processing parameter condition that provides.
Embodiment 1: the Π type radial reactor that goes out on as shown in Figure 4 enterprising, reactor diameter 3m, porous wall inner diameter of steel flue 0.9m, porous wall urceolus diameter 2.7m, bed height 8m.
Embodiment 2: H in the raw material
2The mol ratio of O/ ethylbenzene is 8～10, ethylbenzene liquid air speed is 0.35～0.45h
-1, temperature of reaction is that 550～645 ℃, intake pressure are the ethylbenzene dehydrogenation of 45～80Kpa (absolute pressure), reaction process can adopt any one mode in Fig. 6, Fig. 7, Fig. 8, Fig. 9 or the reactor shown in Figure 10 to implement.
Most preferred embodiment: the mol ratio of H2O/ ethylbenzene is 8 in the raw material, ethylbenzene liquid air speed is that 550～645oC, intake pressure are the ethylbenzene dehydrogenation of 45～60Kpa (absolute pressure) for 0.40h-1, temperature of reaction, and reaction process adopts Fig. 6 or Fig. 8 mode to implement.
Claims (10)
1, a kind of ethylbenzene negative pressure catalytic dehydrogenation preparation of styrene reactive system, comprise at least two catalytic dehydrogenating reaction devices, it is characterized in that, described ethylbenzene catalytic dehydrogenation reactive system employing ∏ type radial reactor and the combination of Z type radial reactor or ∏ type radial reactor and ∏ type radial reactor combine, and wherein have resuperheater to be connected between the outlet and second Reactor inlet of first reactor.
2, ethylbenzene negative pressure catalytic dehydrogenation preparation of styrene reactive system as claimed in claim 1, it is characterized in that, the Z type radial reactor of first reactor for going out on advancing down, second reactor are the ∏ type radial reactor that goes out on enterprising, and resuperheater places the second reactor top.
3, ethylbenzene negative pressure catalytic dehydrogenation preparation of styrene reactive system as claimed in claim 1, it is characterized in that, first reactor is the enterprising Z type radial reactor that goes out down, the ∏ type radial reactor of second reactor for going out under advancing down, and resuperheater places second reactor lower part.
4, ethylbenzene negative pressure catalytic dehydrogenation preparation of styrene reactive system as claimed in claim 1, it is characterized in that, the ∏ type radial reactor of first reactor for going out under advancing down, the Z type radial reactor of second reactor for going out on advancing down, resuperheater places second reactor lower part.
5, ethylbenzene negative pressure catalytic dehydrogenation preparation of styrene reactive system as claimed in claim 1, it is characterized in that, first reactor is the ∏ type radial reactor that goes out on enterprising, and second reactor is the ∏ type radial reactor that goes out on enterprising, and resuperheater places the second reactor top.
6, ethylbenzene negative pressure catalytic dehydrogenation preparation of styrene reactive system as claimed in claim 1, it is characterized in that, the ∏ type radial reactor of first reactor for going out under advancing down, second reactor is the ∏ type radial reactor that advances down to go out down, resuperheater places second reactor lower part.
7, the ∏ type radial reactor that is adopted as each described ethylbenzene negative pressure catalytic dehydrogenation preparation of styrene reactive system in the claim 1 to 6, comprise catalytic bed (5) in a cylindrical vessel (8) and the container, on the top of cylindrical vessel (8) or the same end of bottom reacting gas inlet (1) and reaction gas outlet (2) are set, on cylindrical vessel (8), are provided with catalyzer discharge tube (11); Cylindrical vessel comprises in (8): with the coaxial setting of cylindrical vessel (8), porous wall inner core (6) that is arranged in order from inside to outside and porous wall urceolus (7), porous wall inner core (6) is connected with reacting gas inlet (1), constitute the flow manifold (3) of reactant gases, form annular catalytic bed (5) between porous wall inner core (6) and the porous wall urceolus (7), constitute reactant gases afflux runner (4) between porous wall urceolus (7) and the cylindrical vessel (8), and be connected with reaction gas outlet (2); It is characterized in that the flow direction of reactant gases in afflux runner and flow manifold is opposite, the cross-sectional area ratio of flow manifold and afflux runner is 0.28～2.2.
8, ∏ type radial reactor as claimed in claim 7 is characterized in that, described reactor is provided with the radial flow reactors of cover plate for the catalyst layer top.
9, ∏ type radial reactor as claimed in claim 7 is characterized in that, described reactor does not have the axial-radial flow reactor of cover plate for the catalyst layer top.
10, a kind of method of ethylbenzene negative pressure catalytic dehydrogenation preparation of styrene, it is characterized in that, this method adopts reactive system as claimed in claim 1, the mixed material of ethylbenzene material and high-temperature vapor enters first reactor, behind the beds internal reaction, flow out from first reactor outlet, after resuperheater promotes temperature, enter second reactor, behind the beds internal reaction, flow out, enter interchanger and carry out heat recuperation from second reactor outlet.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2005100231613A CN100509720C (en) | 2005-01-07 | 2005-01-07 | Reacting system and method for preparing styrene by negative pressure ethylbenzene catalytic dehydrogenation |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2005100231613A CN100509720C (en) | 2005-01-07 | 2005-01-07 | Reacting system and method for preparing styrene by negative pressure ethylbenzene catalytic dehydrogenation |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1680227A CN1680227A (en) | 2005-10-12 |
| CN100509720C true CN100509720C (en) | 2009-07-08 |
Family
ID=35067110
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2005100231613A Active CN100509720C (en) | 2005-01-07 | 2005-01-07 | Reacting system and method for preparing styrene by negative pressure ethylbenzene catalytic dehydrogenation |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN100509720C (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104230616B (en) * | 2014-09-29 | 2016-06-08 | 山东齐鲁石化工程有限公司 | Ethyl benzene dehydrogenation preparation of styrene dehydrogenation reactor system |
| CN106693847B (en) * | 2015-08-04 | 2019-01-25 | 中国石化工程建设有限公司 | A kind of micro- catalysis reaction member of radial direction and application thereof |
| CN113620771A (en) * | 2020-05-08 | 2021-11-09 | 中国石油化工股份有限公司 | Reaction system and reaction method for preparing divinylbenzene through dehydrogenation of diethylbenzene |
| CN115452306B (en) * | 2022-09-23 | 2024-03-29 | 中国空气动力研究与发展中心超高速空气动力研究所 | Two-stage series heat accumulating type heater and application method thereof |
-
2005
- 2005-01-07 CN CNB2005100231613A patent/CN100509720C/en active Active
Non-Patent Citations (2)
| Title |
|---|
| 乙苯脱氢缺苯乙烯反应器的技术进展. 徐志刚等人.化学世界，第1卷. 2004 |
| 乙苯脱氢缺苯乙烯反应器的技术进展. 徐志刚等人.化学世界，第1卷. 2004 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1680227A (en) | 2005-10-12 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101254442B (en) | Use of gas-solid catalytic reactor in preparing methanol | |
| CN204841618U (en) | Methanization reactor | |
| CN102029129B (en) | Axial-radial flow gas-solid phase fixed bed catalytic reactor | |
| CN113620244A (en) | System and method for hydrogen production by reforming natural gas steam | |
| CN105032305A (en) | Novel radial plate type reactor | |
| CN204816459U (en) | A methanator that is used for coal system to replace natural gas | |
| CN100509720C (en) | Reacting system and method for preparing styrene by negative pressure ethylbenzene catalytic dehydrogenation | |
| CN101970095A (en) | Catalytic reactor | |
| CN110227394A (en) | A kind of fluidized-bed reactor for Catalyst for Oxidative Coupling of Methane | |
| CN204841617U (en) | Many beds methanator | |
| CN200955019Y (en) | Synthetic multi-section radial cold shock type reactor | |
| CN204816460U (en) | Methane synthesis reactor integrates | |
| CN1259124C (en) | Annular space gas lifting type loop reactor | |
| CN105413592B (en) | A kind of combined type fixed bed reactors and the device formed by it | |
| CN103664497B (en) | Method for producing styrene employing catalytic dehydrogenation of ethylbenzene | |
| CN205235936U (en) | Modular fixed bed reactor reaches device by its formation | |
| CN201088911Y (en) | Radical flow fixed-bed catalytic reactor with multiple heat-exchange modes | |
| CN2499385Y (en) | Radial reactor for preparing synthesis gas by partial oxidation | |
| CN211199063U (en) | Reaction device for catalytic conversion of methanol | |
| CN110003962B (en) | Axial fixed bed methanation reactor | |
| CN1194948C (en) | Method for producing styrene by catalytic dehydrogenation | |
| CN202752008U (en) | Gas phase hydrogenation reactor | |
| CN2243938Y (en) | Multi-layer radial synthetic reactor | |
| CN218931718U (en) | Self-heat-supply type tubular reactor for methanol reforming hydrogen production reaction | |
| CN220182779U (en) | Device for producing hydrogen by methane steam reforming |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |