CN217594571U - Horizontal reactor - Google Patents
Horizontal reactor Download PDFInfo
- Publication number
- CN217594571U CN217594571U CN202021695886.3U CN202021695886U CN217594571U CN 217594571 U CN217594571 U CN 217594571U CN 202021695886 U CN202021695886 U CN 202021695886U CN 217594571 U CN217594571 U CN 217594571U
- Authority
- CN
- China
- Prior art keywords
- horizontal reactor
- reaction space
- reactor according
- liquid
- horizontal
- 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
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
Abstract
The utility model relates to a chemical industry equipment technical field, in particular to horizontal reactor, it includes reaction space, wherein be equipped with catalyst bed and liquid instillation feeding device in the reaction space, liquid instillation feeding device is in including supplying the pipeline that liquid flows and distributing two at least drip wares on the pipeline.
Description
Technical Field
The utility model relates to a chemical industry equipment technical field, in particular to horizontal reactor, it includes reaction space, wherein be equipped with catalyst bed layer and liquid instillation feeding device in the reaction space, liquid instillation feeding device is including supplying the pipeline that liquid flows and distributing two at least drip wares on the pipeline.
Background
Catalytic reactions are often carried out in vertical reactors, and in recent years horizontal reactors have also been increasingly used for catalytic reactions. CN106457188B relates to a horizontal adiabatic reactor for heterogeneous catalytic reactions comprising an outer cylindrical shell, an inlet for reactant gases and an outlet for gaseous products, a basket containing a catalytic bed placed horizontally inside said reactor, wherein said reactor is configured so that the gases pass through said catalytic bed in a radial or axial-radial manner, said shell having a cover which can be opened and which defines an opening, and from which said basket can be extracted horizontally.
CN106660000B, for example, relates to a horizontal reactor for catalytic reactions comprising a cylindrical shell, a catalytic bed and a plurality of heat exchange plates immersed in said catalytic bed, said heat exchange plates being parallel to each other and provided internally with a heat exchange fluid; said reactor comprises a container for said catalytic bed and said heat exchange plates, said container being adapted to be slidingly extracted from said shell, by means of at least one linear guide extending longitudinally with respect to said shell.
For example, CN210825796U relates to an ultraviolet synergetic hydrogen peroxide photocatalytic oxidation high-efficiency reaction device. The reactor comprises a horizontal square stainless steel reactor shell, wherein the reactor shell is provided with a liquid inlet and an outer discharge overflow port, a plurality of ultraviolet lamp tubes are arranged at the top of the reactor shell, the reactor shell is internally divided into three sub-cavities by a partition plate, the first sub-cavity is communicated with the upper part of the second sub-cavity, the second sub-cavity is communicated with the lower part of the third sub-cavity, and a hydrogen peroxide spray head is arranged at the top of the first sub-cavity. The hydrogen peroxide is sprayed on the liquid level in the second cavity, the ultraviolet light directly irradiates on the hydrogen peroxide, the synergistic effect of the ultraviolet light and the hydrogen peroxide is better, the flowing process of the sewage prolongs the photocatalytic oxidation reaction time of the ultraviolet synergistic hydrogen peroxide, and the photocatalytic degradation efficiency of organic matters in the sewage is improved.
SUMMERY OF THE UTILITY MODEL
For some reactors adopting a horizontal or large-area flat-laying mode, reaction raw materials contain liquid-phase raw materials, but the filling flux of the liquid-phase raw materials is low, only the surfaces of solid particles of a catalyst need to be soaked, and liquid phases are not expected to fill a reactor cavity to form accumulated liquid. For such liquid phase raw materials, the conventional single-point feeding mode easily causes a long distribution path and a long infiltration time of the liquid phase raw materials, and the reaction efficiency and the effect are seriously influenced.
The utility model discloses an inventor has designed a horizontal reactor through the research, and this kind of reactor has compensatied the not enough of prior art, provides an use the distributed reactor structure of instilling feeding device for the liquid phase raw materials can be in the catalyst is annotated with the form that evenly distributed instilled in the horizontal cross section direction, and can control the liquid phase effectively and not produce the hydrops when infiltrating the catalyst.
The utility model discloses a horizontal reactor includes the reaction space, be equipped with catalyst bed and the instillation feeding device of liquid in the reaction space, the liquid instills feeding device including the pipeline that supplies liquid to flow and distributes two at least instillations ware on the pipeline, horizontal reactor still has the gas permeability component, the reaction space by horizontal reactor shell and be located the gas permeability component of horizontal reactor one side and be located horizontal reactor in with the gas permeability component of the opposite side that one side is relative is injectd and is formed, reaction gas follows one side gets into the reaction space, and product gas follows the reaction space is left to the opposite side, the gas permeability component of one side constructs out the air inlet chamber with the horizontal reactor shell of homonymy, the gas permeability component of opposite side constructs out the air outlet chamber with the horizontal reactor shell of homonymy, is connected with admission line, the pipeline of giving vent to anger on air inlet chamber, the air outlet chamber respectively.
Drawings
The present invention will be further described with reference to the accompanying drawings.
Fig. 1A and 1B are a horizontal view and a top perspective view, respectively, of a preferred embodiment of the present invention;
fig. 2 is a top perspective view of another preferred embodiment of the present invention;
fig. 3A and 3B show a horizontal view and a top view, respectively, of a preferred embodiment of the drip chamber of the present invention.
In the figure, 1-pipeline inlet of pipeline, 2a and 2 b-air permeability component, 3-gas phase raw material, 4-air inlet chamber, 5-heat preservation layer, 6-drip chamber, 7-drain port, 8-air outlet chamber, 9-gas phase product, 10-horizontal reactor, 11-pipeline, 12-flat-bed reactor and 13-multi-row pipeline.
Detailed Description
The utility model provides an use and drip irrigation feeding device's reactor structure for the liquid phase raw materials can be in the catalyst is annotated with the form that evenly distributed driped irrigation in the horizontal cross section direction, and can control the liquid phase effectively and not produce the hydrops when infiltrating the catalyst.
Before further describing the present invention, certain terms used in the specification, examples, and appended claims are collected in the following sections. The definitions set forth herein should be read and understood by those skilled in the art in view of the remainder of the present disclosure. Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs.
The terms "a" and "an" are used herein for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated.
The term "about" as used herein when referring to a value is meant to encompass variations thereof, such as ± 10%, ± 5%, ± 1%, or ± 0.1% of the specified value.
The term "substantially full" as used herein means occupying more than 95%, preferably more than 98%, more preferably more than 99% of the total volume.
In a specific embodiment, the horizontal reactor of the present invention comprises a reaction space, wherein a catalyst bed and a liquid instillation feeding device are disposed in the reaction space, and the liquid instillation feeding device comprises a pipeline for liquid to flow and at least two instillers distributed on the pipeline.
In one embodiment, the catalyst bed occupies more than 50%, preferably more than 75%, more preferably more than 90% of the reaction space, and most preferably the catalyst bed substantially fills the reaction space.
In one embodiment, the liquid instillation feeding device is arranged at the upper part of the reaction space in a direction parallel to the bottom surface of the horizontal reactor, and the height of the central axis of the pipeline of the liquid instillation feeding device from the bottom of the reaction space is 1/2 to 1 time, preferably 3/4 to 1 time of the total height of the reaction space.
In one embodiment, the catalyst particles have an average diameter of from about 1nm to about 50 μm, preferably from about 100nm to about 10 μm, from about 500nm to about 10 μm, or from about 500nm to about 2 μm.
In one embodiment, the catalyst particles comprise a metal, oxide, sulfide, carbide, preferably comprising Co, fe, al, ag, au, pt, cu, ni, zn, ti, mn, C, pd, ru, titania, zinc oxide, tin oxide, zirconia, cadmium sulfide, preferably the catalyst particles are composite catalysts.
In one embodiment, the catalyst packing density is about 0.1g/cm 3 To about 10g/cm 3 Preferably about 0.5g/cm 3 To about 5g/cm 3 More preferably about 1g/cm 3 To about 2g/cm 3 。
In a particular embodiment, the number of drip chambers is from 2 to 50, preferably from 5 to 20, more preferably from 8 to 12.
In one embodiment, the drip chambers are evenly distributed at the bottom of the tubing.
In one embodiment, the drip chamber is of an inverted cone shape, wherein the outlet end cone diameter of the drip chamber is fixed and the outlet end cone diameter is from about 0.1mm to about 2mm, preferably from about 0.5mm to about 1mm.
In one embodiment, the drip chamber is in an inverted cone shape, wherein the size of the outlet end cone mouth of the drip chamber can be adjusted in an opening and closing manner, and the size of the outlet end cone mouth can be continuously changed within 0.1mm to 2mm, preferably 0.5mm to 1mm. In a preferred embodiment, the drip chamber is composed of a plurality of blades and an external inverted cone nut, wherein the blades are surrounded in the circumferential direction and sequentially compressed, the blades are screwed or unscrewed by rotating the inverted cone nut, and the opening and closing of the liquid outlet end of the drip chamber are adjusted.
In one embodiment, the diameter of the inlet cone of each drip chamber is 1mm to 10mm, preferably 3mm to 6mm, and the perpendicular distance between the plane of the inlet cone and the plane of the outlet cone is 3mm to 15mm, preferably 5mm to 10mm.
In a specific embodiment, each of the drip chambers allows dripping at a rate of 0.1 to 10mL/min, preferably 0.5 to 2mL/min, more preferably 0.5 to 1 mL/min.
In a particular embodiment, the tubes may be arranged in a single row, in a plurality of rows, in a mesh and/or in a ring, wherein in the case of a plurality of rows, only one tube inlet is provided on the tubes, the rows being parallel to one another and one end of each row being interconnected by a header and/or the other end of each row being interconnected by a further header, such that liquid can flow from the header and/or the further header to each row.
In one embodiment, the line inlet of the conduit is located outside the reaction space.
In a specific embodiment, the horizontal reactor further comprises a gas permeable member, preferably a sintered metal plate, the reaction space is defined by a horizontal reactor shell, the gas permeable member is located on one side of the horizontal reactor, the gas permeable member is located on the other side of the horizontal reactor, the reaction gas enters the reaction space from the one side, the product gas leaves the reaction space from the other side, the gas permeable member on the one side and the horizontal reactor shell on the same side form an inlet chamber, the gas permeable member on the other side and the horizontal reactor shell on the same side form an outlet chamber, and the inlet chamber and the outlet chamber are respectively connected with an inlet pipeline and an outlet pipeline.
In one embodiment, the horizontal reactor has a hydrophobic port in the bottom of the reaction space.
In one embodiment, the reaction space has an insulating layer inside and/or outside.
In one embodiment, the horizontal reactor has a temperature control device.
In one embodiment the ratio of the inlet gas flow rate to the inlet liquid flow rate is a molar ratio 5:1 to 1:3, preferably 3:1 to 1:2, more preferably 2:1 to 1:1, the temperature in the horizontal reactor is controlled to be 20 ℃ to 250 ℃, preferably 60 ℃ to 180 ℃, more preferably 100 ℃ to 150 ℃, and the pressure is controlled to be 1 to 20 atmospheres, preferably 1 to 10 atmospheres, more preferably 3 to 7 atmospheres.
In one embodiment, the reaction space further comprises a liquid level monitoring device.
In one embodiment, the horizontal reactor is a horizontal reactor.
In one embodiment, the horizontal reactor has a volume of 1L to 3000L, preferably 10L to 1000L, more preferably 100L to 300L.
In one embodiment, the cross-sectional shape of the horizontal reactor parallel to the bottom surface is rectangular, square, circular or elliptical, preferably rectangular.
Example 1
As shown in fig. 1A and 1B, the horizontal reactor includes a shell and a reaction space, a heat insulating layer is arranged on the periphery of the reaction space, sintered metal plates are arranged on the left and right sides of the reaction space, an air inlet chamber and an air outlet chamber are respectively constructed by the wall and the sintered metal plates on the left and right sides, the air inlet chamber and the air outlet chamber are respectively connected with an air inlet pipeline and an air outlet pipeline, a catalyst bed layer and a liquid instillation feeding device which is arranged on the upper portion of the reaction space in an extending manner along the direction parallel to the bottom surface of the horizontal reactor are arranged in the reaction space, a drain hole is arranged at the bottom in the reaction space, wherein the catalyst bed layer accounts for 80% of the reaction space, and the height of the central axis of the pipeline of the liquid instillation feeding device from the bottom of the reaction space is 3/4 of the total height of the reaction space.
The catalyst particles used were a metal oxide composite catalyst and had an average diameter of 1 μm and a catalyst loading density of 1.6g/cm 3 . The catalyst has a certain supporting structure and is loosely filled in a solid state in the reactor.
The liquid instillation feeding device comprises a single-row pipeline and 6 instillators uniformly arranged at the bottom of the single-row pipeline. The structure of the drip chamber is as shown in fig. 3A and 3B, the drip chamber is designed in an inverted cone shape and is composed of a plurality of blades and an external inverted cone nut, the blades are surrounded in the circumferential direction and sequentially compressed, the blades are screwed or unscrewed through rotation of the inverted cone nut, and the size of the drip chamber is adjusted to be opened or closed. The diameter of the liquid inlet end cone of the drip chamber is 3mm, the diameter of the liquid outlet end cone can be continuously changed within the range of 0.3mm to 0.5mm, the dripping speed of each drip chamber is 0.7-0.8mL/min, and the drip chamber is used for adding liquid water as a reactant.
The gas inlet chamber and the gas outlet chamber are arranged at the left end and the right end of the reactor, are isolated from the reaction space by a sintered metal plate, and are filled with raw material gas CO 2 The gas inlet pipeline is introduced into the reaction space through the gas inlet chamber and the sintered metal plate to be uniformly contacted with the catalyst on the catalyst bed layer; the gas phase hydrocarbon product passes through the sintered metal plate at the other end of the reaction space and the exhaust chamber and is exhausted by the exhaust pipeline.
The bottom in the reactor is provided with a drain port and a condensed water drainer to help the unvaporized raw material liquid and a small amount of condensate liquid of the product to be discharged, so as to avoid forming accumulated liquid in the reaction cavity.
The ratio of the inlet flow rate to the inlet flow rate is 1:1, the temperature in the reactor is controlled at 130 ℃, and the pressure is 5 atmospheric pressures.
Example 2
As shown in fig. 2, the tiled reactor includes a shell and a reaction space, a heat insulating layer is arranged on the periphery of the reaction space, sintered metal plates are arranged on the left and right sides of the reaction space, an air inlet chamber and an air outlet chamber are respectively formed by the wall and the sintered metal plates on the left and right sides, an air inlet pipeline and an air outlet pipeline are respectively connected to the air inlet chamber and the air outlet chamber, a catalyst bed layer and a liquid instillation feeding device which is arranged on the upper portion of the reaction space and extends in a direction parallel to the bottom surface of the horizontal reactor are arranged in the reaction space, a drain hole is arranged at the bottom in the reaction space, wherein the catalyst bed layer accounts for 80% of the reaction space, and the height of the central axis of the pipeline of the liquid instillation feeding device from the bottom of the reaction space is 3/4 of the total height of the reaction space.
The catalyst particles are metal oxide composite catalyst, the average diameter is 1 μm, and the catalyst loading density is 1.6g/cm 3 . The catalyst has a certain supporting structure and is loosely filled in a solid state in the reactor.
Liquid instillation feeding device includes pipeline and 36 drip chamber only set up a pipeline entry on the pipeline, the pipeline is six rows of arranging, and drip chamber evenly distributed sets up in the bottom of six rows, six rows are parallel to each other just one end and the other end of six rows are respectively through house steward interconnect, so that liquid can follow house steward flow direction is respectively arranged. Each drip chamber is designed in an inverted cone shape, the diameter of a cone at a liquid inlet end is 3mm, the diameter of a cone at a liquid outlet end is 0.5mm, and the dripping speed of each drip chamber is 0.5mL/min, and is used for adding liquid water as a reactant.
The gas inlet chamber and the gas outlet chamber are arranged at two ends of the reactor, are isolated from the reaction space by a sintered metal plate, and are filled with raw material gas CO 2 The gas inlet pipeline is introduced into the inner cavity of the reactor through the gas inlet chamber and the sintered metal plate to be in uniform contact with the catalyst; the gas phase hydrocarbon product is discharged from the gas discharge pipeline through the metal plate sintered at the other end of the inner cavity of the reactor and the gas discharge chamber.
The bottom in the reactor is designed with a condensed water drainer arranged at the drain hole, which helps the unvaporized raw material liquid and a small amount of condensate of the product to be discharged, and avoids the formation of accumulated liquid in the reaction cavity.
The ratio of the inlet flow rate to the inlet flow rate is 1:1, the temperature in the reactor is controlled at 130 ℃, and the pressure is 5 atmospheric pressures.
In this specification and the appended claims, the singular forms "a", "an" and "the" include plural referents unless the context clearly dictates otherwise. Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art. The methods described herein may be performed in any order that is logically possible, except in the particular order disclosed.
The representative examples are intended to aid in the description of the invention and are not intended to, nor should they be construed as, limiting the scope of the invention. Indeed, various modifications of the invention and many other embodiments thereof, in addition to those shown and described herein, will become apparent to those skilled in the art, including the examples and scientific and patent literature references cited herein. The embodiments contain important additional information, exemplification and guidance which can be employed by the practice of the invention in its various embodiments and equivalents.
Claims (32)
1. The utility model provides a horizontal reactor, its includes the reaction space, its characterized in that, be equipped with catalyst bed and liquid instillation feeding device in the reaction space, liquid instillation feeding device is including supplying liquid mobile pipeline and distribution at least two instillators on the pipeline, horizontal reactor still has the gas permeability component, the reaction space is injectd by horizontal reactor shell and the gas permeability component that is arranged in horizontal reactor one side and the gas permeability component that is arranged in horizontal reactor with the opposite side of one side and forms, and reacting gas follows one side gets into the reaction space, and the resultant gas is followed the reaction space is left to the opposite side, the gas permeability component of one side and the horizontal reactor shell of homonymy construct the inlet chamber, the gas permeability component of opposite side constructs out the outlet chamber with the horizontal reactor shell of homonymy, is connected with inlet line, the pipeline of giving vent to anger on inlet chamber, the outlet chamber respectively.
2. The horizontal reactor according to claim 1, wherein the catalyst bed occupies more than 50% of the reaction space.
3. The horizontal reactor according to claim 2, wherein the catalyst bed occupies more than 75% of the reaction space.
4. The horizontal reactor according to claim 2, wherein the catalyst bed occupies more than 90% of the reaction space.
5. The horizontal reactor according to claim 2, wherein the catalyst bed substantially fills the reaction space.
6. The horizontal reactor according to any one of claims 1 to 5, wherein the liquid instillation feeding device is extended in a direction parallel to the bottom surface of the horizontal reactor and is disposed in the upper part of the reaction space, and the height of the central axis of the pipe of the liquid instillation feeding device from the bottom of the reaction space is 1/2 to 1 time of the total height of the reaction space.
7. A horizontal reactor according to claim 6 wherein the central axis of the conduit of the liquid instillation feed device is at a height from the bottom of the reaction space of from 3/4 to 1 times the total height of the reaction space.
8. The horizontal reactor according to any one of claims 1 to 5, wherein the catalyst particles have an average diameter of about 1nm to about 50 μm.
9. The horizontal reactor of claim 8, wherein the catalyst particles have an average diameter of about 100nm to about 10 μm.
10. The horizontal reactor of claim 8, wherein the catalyst particles have an average diameter of about 500nm to about 10 μm.
11. The horizontal reactor of claim 8, wherein the catalyst particles have an average diameter of about 500nm to about 2 μm.
12. The horizontal reactor of any one of claims 1-5, wherein the catalyst packing density is about 0.1g/cm 3 To about 10g/cm 3 。
13. The horizontal reactor of claim 12, wherein the catalyst packing density is about 0.5g/cm 3 To about 5g/cm 3 。
14. The horizontal reactor of claim 12, wherein the catalyst packing density is about 1g/cm 3 To about2g/cm 3 。
15. The horizontal reactor according to any one of claims 1 to 5, wherein the number of the drip chambers is 2 to 50.
16. The horizontal reactor according to claim 15, wherein the number of the drip chambers is 5 to 20.
17. The horizontal reactor according to claim 15, wherein the number of the drip chambers is 8 to 12.
18. The horizontal reactor according to any one of claims 1 to 5, wherein the drip chambers are uniformly distributed at the bottom of the pipe.
19. The horizontal reactor according to any one of claims 1 to 5, wherein the drip chamber is in the shape of an inverted cone, wherein the outlet end cone of the drip chamber has a fixed diameter, and the outlet end cone has a diameter of about 0.1mm to about 2mm.
20. The horizontal reactor according to claim 19 wherein the exit end cone has a diameter of about 0.5mm to about 1mm.
21. The horizontal reactor according to any one of claims 1 to 5, wherein the drip chamber is in an inverted cone shape, the ruler diameter of the liquid outlet end cone mouth of the drip chamber can be adjusted in an opening and closing mode, and the ruler diameter of the liquid outlet end cone mouth can be continuously changed within 0.1mm to 2mm.
22. The horizontal reactor as claimed in claim 21, wherein the size of the outlet end cone is continuously variable within 0.5mm to 1mm.
23. The horizontal reactor according to any one of claims 1 to 5, wherein the diameter of the inlet cone of each drip chamber is 1mm to 10mm, and the perpendicular distance between the plane of the inlet cone and the plane of the outlet cone is 3mm to 15mm.
24. The horizontal reactor according to claim 23, wherein each drip chamber has a diameter of the inlet cone of 3mm to 6mm and a vertical distance of the plane of the inlet cone from the plane of the outlet cone of 5mm to 10mm.
25. A horizontal reactor according to any one of claims 1 to 5 wherein the tubes are arranged in a single row, multiple rows, mesh and/or ring, wherein when the tubes are arranged in multiple rows, only one tube inlet is provided in the tubes, the multiple rows are parallel to each other and one end of each row is interconnected by a header and/or the other end of each row is interconnected by another header, such that liquid can flow from the header and/or the other header to each row.
26. A horizontal reactor according to any one of claims 1 to 5, wherein the pipe inlet of the pipe is located outside the reaction space.
27. The horizontal reactor according to claim 1, wherein the gas permeable member is a sintered metal plate.
28. The horizontal reactor according to any one of claims 1 to 5, wherein the horizontal reactor has a hydrophobic port in the bottom of the reaction space.
29. A horizontal reactor according to any one of claims 1 to 5, wherein the reaction space is internally and/or externally provided with an insulating layer.
30. The horizontal reactor according to any one of claims 1 to 5, wherein the horizontal reactor is provided with a temperature control device.
31. A horizontal reactor according to any one of claims 1 to 5 wherein a liquid level monitoring device is also provided in the reaction space.
32. The horizontal reactor according to any one of claims 1 to 5, wherein the horizontal reactor is a tiled reactor.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202021695886.3U CN217594571U (en) | 2020-08-14 | 2020-08-14 | Horizontal reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202021695886.3U CN217594571U (en) | 2020-08-14 | 2020-08-14 | Horizontal reactor |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN217594571U true CN217594571U (en) | 2022-10-18 |
Family
ID=83561754
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202021695886.3U Active CN217594571U (en) | 2020-08-14 | 2020-08-14 | Horizontal reactor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN217594571U (en) |
-
2020
- 2020-08-14 CN CN202021695886.3U patent/CN217594571U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN1009057B (en) | Multitube reactor | |
| JP4651889B2 (en) | Isothermal reactor for exothermic or endothermic heterogeneous reactions | |
| KR101558406B1 (en) | Vessel for containing catalyst in a tubular reactor | |
| RU2007125987A (en) | REACTOR PIPE DEVICE | |
| CN102397709B (en) | Modular catalyst filling structure of vertical sieve plate | |
| CN1638856A (en) | Reactor and method for producing phosgene | |
| CN100551478C (en) | Catalyze rectification packing tower | |
| CN102481539A (en) | Reactor for exothermic or endothermic catalytic reactions | |
| CN212390878U (en) | Winding pipe heat exchanger with pipe pass capable of being cleaned on line | |
| CN105008037A (en) | Device and method for the continuous reaction of liquids with gases | |
| CN217594571U (en) | Horizontal reactor | |
| CN200955019Y (en) | Synthetic multi-section radial cold shock type reactor | |
| US5262130A (en) | Fixed bed chemical reactor | |
| CN112427002B (en) | Tower-type superfine contact reaction device for biodiesel | |
| JP3739903B2 (en) | Gas-liquid dispersion device, gas-liquid contact device, and wastewater treatment device | |
| CN212843054U (en) | Multi-strand flow wound tube heat exchanger with tube pass capable of being cleaned on line | |
| CN218131816U (en) | Photochemical reactor reaction liquid shunting structure and photochemical reactor | |
| CN107224947A (en) | A kind of micro passage reaction | |
| RU2381057C2 (en) | Reaction vessel | |
| CN114797519A (en) | Constant temperature liquid source bubbler | |
| CN105776141A (en) | Novel fixed bed reactor for preparing chlorine gas through catalytic oxidation of hydrogen chloride | |
| CN201807351U (en) | Gas distributor with bent pore channels and carbonylation acetic acid and acetic anhydride cogeneration synthetic tower based on gas distributor | |
| CN114522514A (en) | Gas phase quenching circulating absorption tower for preparing acrylic acid by propylene oxidation method | |
| CN207446202U (en) | A kind of fluidized-bed reactor | |
| US20030086846A1 (en) | Monolith stacking configuration for improved flooding |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |