CN205127915U - Trickle bed reactor - Google Patents
Trickle bed reactor Download PDFInfo
- Publication number
- CN205127915U CN205127915U CN201520786158.6U CN201520786158U CN205127915U CN 205127915 U CN205127915 U CN 205127915U CN 201520786158 U CN201520786158 U CN 201520786158U CN 205127915 U CN205127915 U CN 205127915U
- Authority
- CN
- China
- Prior art keywords
- gas
- passage pipe
- bed reactor
- short tube
- distribution grid
- 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
Landscapes
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The utility model relates to a trickle bed reactor, the reactor includes gas -liquid distributor, gas -liquid distributor includes distributing plate, gas passage pipe and fluid passage pipe, the gas passage pipe is including the circular cone top cap and the nozzle stub of standing vertically, the circular cone top cap with upright form the space of air feed body business turn over between the upper end of nozzle stub, upright the lower extreme of nozzle stub set up in on the distributing plate, the fluid passage pipe is perpendicular nozzle stub, perpendicular nozzle stub runs through the distributing plate, be located the aperture is evenly opened to the perpendicular nozzle stub part of distributing plate below crisscrossly on the cross section along the different positions of axial, gas passage pipe evenly distributed in the fluid passage intertube, wherein, perpendicular nozzle stub is located the part of distributing plate below, its end links to each other with the stream breaker, the stream breaker includes the round hole of center department and describes a seam along dispersing of circumference evenly distributed.
Description
Technical field
The utility model relates to a kind of trickle bed reactor.
Background technology
Trickle bed reactor is one of main several reactors, because it had both had the advantage that structure is simple, equipment investment is low, has again easy to operate, that operating flexibility is large feature, is therefore widely used at oil refining, chemical field.In trickle bed reactor, gas and liquid also flow through beds, and wherein liquid flows through beds with trickle flow, and gas is then pass through in the mode of continuous-flow.Therefore, the uniformity that can liquid form drip in reactor, whether distribution of gas evenly directly affects reactant and catalyst contact time, affects the degree that catalyst surface is soaked by liquid phase.And gas-liquid skewness can form the phenomenon such as bias current and partial short-circuit, finally can affect the performance of catalyst action, affect the quality of product, therefore the importance of gas-liquid dielectric distribution is more outstanding.
Trickle bed reactor adopts gas-liquid allotter gas-liquid homogeneous media to be assigned on the beds of below usually.The usual length pipe of existing gas-liquid allotter is divided three classes: overflow type, suction type and the two mixed type.As a kind of overflow type distributor that document CN200710039071.2 mentions, mainly have part aperture in the surrounding of liquid-phase tube, solve liquid and gas only there is axial flow to distribute and be difficult to be formed the problem that even gas-liquid distributes, but when still there is liquid outflow main body tube in this distributor, drop is comparatively large, even has the shortcoming of central bus phenomenon.Document CN20042011597.2 discloses a kind of suction type gas-liquid allotter, this distributor has set up isocon on the basis of traditional suction type gas-liquid allotter, reduce gas-liquid allotter gas-liquid allotter gas-liquid allotter pressure drop, improve in gas-liquid distribution effects and have certain effect.But this dispensing arrangement more complicated, manufacturing cost are high and the troublesome shortcoming of installation and repairing.The gas-liquid allotter disclosing a kind of suction type and overflow type combination of document CN98250778.X, this kind of distributor is provided with the crushing shell of the symmetrical bar seam of band at traditional drawing-in type gas-liquid allotter central tube root edge, the spray area of the liquid increased to a certain extent, improve the distributed effect of gas-liquid (particularly high viscosity medium), but the crushing shell of this distributor only has strip bar seam along the surrounding of crushing shell, still there is the center stream not easily disperseed in crushing shell central lower region, and this structure of distributor is complicated, installation and repairing trouble.
Summary of the invention
Technical problem to be solved in the utility model is that prior art exists gas-liquid problem pockety, provides a kind of new trickle bed reactor.This trickle bed reactor has the feature of uniform gas-liquid distribution.
For solving the problems of the technologies described above, the technical solution adopted in the utility model is as follows: a kind of trickle bed reactor, comprises housing, gas pre-distributor, liquid pre-distributor, gas-liquid allotter, gas-phase product outlet and liquid product outlet; Described gas-liquid allotter comprises distribution grid, gas passage pipe and fluid passage pipe;
Described gas passage pipe comprises circular cone top cover and upright short tube; The space that supplied gas passes in and out is formed between the upper end of described circular cone top cover and described upright short tube; The lower end of described upright short tube is arranged on described distribution grid;
Described fluid passage pipe is vertical short tube, and described vertical short tube runs through described distribution grid; Be positioned at vertical short tubular portions below described distribution grid and evenly have aperture alternately on the cross section of diverse location vertically;
Described gas passage pipe is uniformly distributed between described fluid passage pipe;
Wherein, described vertical short tube is positioned at the part below described distribution grid, and its end is connected with stream breaker; Described stream breaker comprises the circular hole of center, and circumferentially equally distributed divergent shape bar stitches.
In technique scheme, preferably, the divergent shape bar seam on described stream breaker is rectangle or triangle.
In technique scheme, preferably, the divergent shape bar on described stream breaker is sewed with 3 ~ 6.
In technique scheme, preferably, the rate of cracking of the divergent shape bar seam on described stream breaker is 10 ~ 40%.
In technique scheme, preferably, the described vertical short tube part be positioned at above described distribution grid accounts for 3 ~ 20% of described vertical short tube total length.
In technique scheme, preferably, described vertical short tube is positioned at the part below described distribution grid is 200 ~ 1000 millimeters.
In technique scheme, preferably, the percent opening of described gas passage pipe on described distribution grid is 10 ~ 30%.
In technique scheme, preferably, the percent opening of described fluid passage pipe on described distribution grid is 10 ~ 50%.
In technique scheme, preferably, the gas passage pipe on described distribution grid and fluid passage pipe are equilateral triangle arrangement.
In technique scheme, preferably, the diameter d of described aperture is 3 ~ 8mm, in foraminate gross area S1 and fluid passage pipe the ratio of sectional area S2 be (0.75:1) ~ (1:1).
In technique scheme, preferably, described gas pre-distributor is arranged at described reactor head, and described liquid pre-distributor is arranged at housing side surface upper part, described gas-phase product outlet is arranged at case side basifacial, and described liquid product outlet is arranged at described reactor bottom.
In the utility model trickle bed reactor, described gas-liquid allotter is arranged under gas pre-distributor and liquid pre-distributor.When the utility model trickle bed reactor is used for gas liquid reaction, catalyst can be filled with in reactor shell.The type of feed of catalyst is for known in the art, generally in housing, is disposed with top porcelain ball, beds, bottom porcelain ball and supporting screening plate below gas-liquid allotter.Usually, gas-liquid allotter is 400 ~ 1200mm apart from the distance of top porcelain ball.
Compared with prior art, the gas-liquid allotter of the utility model trickle bed reactor is provided with connected stream breaker at the vertical short tube portion distal end be positioned at below distribution grid, on the one hand gas-liquid allotter of the present invention not only remain former overflow type gas-liquid allotter structure simple, the advantage such as intensively can to arrange; On the other hand, gas-liquid allotter of the present invention is by setting up stream breaker at the vertical short tube end of main body of liquid, circular hole is had by the center at stream breaker, circumferentially have equally distributed divergent shape bar seam, not only considerably increase the spray area of liquid, and eliminate one center not easily the disperseed stream existed in crushing shell central lower region, thus guarantee that large drop is fractured into fine mist, under the drive of gas, spray in spray pattern, substantially improve gas-liquid distribution situation.To the recyclegas of NO be contained in the mixing material containing nitric acid, first alcohol and water of oxidative esterification tower tower reactor discharge in synthesis gas preparing ethylene glycol technology and CO coupling system and circulate in described trickle bed reactor, ensure that preferably gas containing NO and the liquid containing nitric acid, methyl alcohol enter reactor after being uniformly distributed on whole bed cross section, give full play to the effect of catalyst, ensure that the conversion ratio of nitric acid preferably, reaching turns waste into wealth and lower consumption subtracts rotten object.Adopt trickle bed reactor of the present utility model, in reactor Raney nickel effect under, be 70 ~ 120 DEG C in reaction temperature, reaction pressure is 0 ~ 1.5MPa, and liquid hourly space velocity (LHSV) is 0.5 ~ 8 hour
-1, the mol ratio of NO and nitric acid is react under the condition of 2.5 ~ 10 to generate methyl nitrite, nitric acid conversion ratio>=95%, achieves good technique effect.
Accompanying drawing explanation
Fig. 1 is the schematic diagram of the utility model trickle bed reactor.
Fig. 2 is the A-A sectional top view of the utility model trickle bed reactor.
Fig. 3-1 is gas-liquid allotter sectional view in the utility model trickle bed reactor.
Fig. 3-2 is gas-liquid allotter stream breaker (17) schematic diagram with two kinds of forms.
Fig. 3-3 is the gas passage pipe schematic diagram of gas-liquid allotter.
Fig. 3-4 is the fluid passage pipe schematic diagram of gas-liquid allotter.
Symbol description: 1 is housing, 2 is gas pre-distributor, 3 is liquid pre-distributor, 4 is the gas passage pipe of gas-liquid allotter, 5 is the distribution grid of gas-liquid allotter, 6 is the fluid passage pipe of gas-liquid allotter, 7, 9 is porcelain ball, 8 is beds, 10 is supporting screening plate, 11 is gas-phase product outlet, 12 is liquid product outlet, 13 is the circular cone top cover of gas-liquid allotter gas passage pipe, 14 is the upright short tube of gas-liquid allotter gas passage pipe, 15 is the vertical short tube of gas-liquid allotter fluid passage pipe, 16 is the aperture on the vertical short tube of gas-liquid allotter fluid passage pipe, 17 is stream breaker.
The operation principle of the utility model trickle bed reactor in Fig. 1: the mixing material containing nitric acid, first alcohol and water enters trickle bed reactor through liquid pre-distributor (3), the mist containing NO enters trickle bed reactor through gas pre-distributor (2).Liquid through liquid pre-distributor (3) initial distribution enters the fluid passage pipe (6) of gas-liquid allotter, flow out through the vertical short tube of fluid passage pipe (15) side aperture (16), form the transverse annular distribution of liquid; Meanwhile, liquid is after stream breaker (17) effect bottom fluid passage pipe, and large drop is fractured into fine mist, sprays downwards in spray pattern, forms the axial distribution of liquid.Gas after gas pre-distributor (2) initial distribution enters the gas passage pipe (4) of gas-liquid allotter, gas flows into from the annular space formed between the circular cone top cover (13) and upright short tube (14) upper end of gas passage pipe, forms axial distribution of gas; Meanwhile, the vertical short tube (15) of fluid passage pipe is not full liquid, and aperture (16) supplied gas at the vertical short tube top of fluid passage pipe flows out, and forms horizontal annular gas distribution.So, gas-liquid two-phase enters beds through top porcelain ball (7), react under the effect of catalyst, product enters reactor lower part space behind bottom porcelain ball (9), finally, reaction gas-phase product is drawn through gas-phase product outlet (11), and reaction liquid product is drawn through liquid product outlet (12).
In Fig. 2, gas passage pipe is uniformly distributed between fluid passage pipe, and the gas passage pipe on distribution grid and fluid passage pipe are equilateral triangle arrangement.
In Fig. 3-1, gas-liquid allotter, comprises distribution grid, gas passage pipe and fluid passage pipe.Gas passage pipe comprises circular cone top cover and upright short tube; The space that supplied gas passes in and out is formed between the upper end of circular cone top cover and upright short tube; The lower end of upright short tube is arranged on distribution grid.Fluid passage pipe is vertical short tube, and vertical short tube runs through distribution grid; Be positioned at vertical short tubular portions below distribution grid and evenly have aperture alternately on the cross section of diverse location vertically.Wherein, the portion distal end that vertical short tube is positioned at below distribution grid is connected with stream breaker.
In Fig. 3-2, stream breaker comprises the circular hole of center, and circumferentially equally distributed divergent shape bar stitches.Divergent shape bar seam is rectangle or triangle.Divergent shape bar is sewed with 3 ~ 6.The rate of cracking of divergent shape bar seam is 10 ~ 40%.
In Fig. 3-3, gas passage pipe comprises circular cone top cover and upright short tube; The space that supplied gas passes in and out is formed between the upper end of circular cone top cover and upright short tube.Gas flows into from the annular space formed between circular cone top cover and upright upper end of short tube, flows out from the lower end of upright short tube, forms axial distribution of gas.
In Fig. 3-4, liquid enters the fluid passage pipe of gas-liquid allotter, flows out through fluid passage pipe vertical short tube side aperture, forms the transverse annular distribution of liquid; Meanwhile, liquid is after the stream breaker effect bottom fluid passage pipe, and liquid phase is that spray pattern sprays downwards, forms the axial distribution of liquid.
Below by embodiment, the utility model is further elaborated.
Detailed description of the invention
[embodiment 1]
By Fig. 1, Fig. 2, Fig. 3-1, Fig. 3-2, Fig. 3-3 and Fig. 3-4, the catalyst in trickle bed reactor adopts nickel catalyst, the gas passage pipe of the gas-liquid allotter in reactor and fluid passage pipe are equilateral triangle arrangement, and the percent opening of gas passage pipe on distribution grid is 10%, and the percent opening of fluid passage pipe on distribution grid is 10%, the part of short tube above distribution grid of fluid passage pipe accounts for 20% of described vertical short tube total length, short tube lower end to stretch out below distribution grid 200 millimeters, the short tubular portions be positioned at below distribution grid circumferentially evenly has aperture, the diameter d of aperture is 3mm, in foraminate gross area S1 and fluid passage pipe the ratio of sectional area S2 be 0.75:1, the stream breaker center be connected with short tube end have circular aperture 1, circumferentially equally distributed rectangular opening 3, the percent opening of the broken discharge orifice on stream breaker is 10%, the distance that gas-liquid allotter is arranged at apart from reactor top porcelain ball is 400mm.The mixing material containing nitric acid, water and methyl alcohol of oxidative esterification tower tower reactor being discharged and the mist containing NO pass into above-mentioned trickle bed reactor respectively, and be 70 DEG C in reaction temperature, reaction pressure is normal pressure, and liquid hourly space velocity (LHSV) is 0.5h
-1, the mol ratio of NO and nitric acid is the generation methyl nitrite that reacts under the condition of 5, and the conversion ratio of nitric acid is 95.2%.
[embodiment 2]
By Fig. 1, Fig. 2, Fig. 3-1, Fig. 3-2, Fig. 3-3 and Fig. 3-4, the catalyst in trickle bed reactor adopts nickel catalyst, the gas passage pipe of the gas-liquid allotter in reactor and fluid passage pipe are equilateral triangle arrangement, and the percent opening of gas passage pipe on distribution grid is 15%, and the percent opening of fluid passage pipe on distribution grid is 20%, the short tube of fluid passage pipe accounts for 10% of described vertical short tube total length in the part above distribution grid, short tube lower end to stretch out below distribution grid 500 millimeters, the short tubular portions be positioned at below distribution grid circumferentially evenly has aperture, the diameter d of aperture is 4mm, in foraminate gross area S1 and fluid passage pipe the ratio of sectional area S2 be 1:1, the stream breaker center be connected with short tube end have circular aperture 1, circumferentially equally distributed rectangular opening 4, the percent opening of the broken discharge orifice on stream breaker is 20%, the distance that gas-liquid allotter is arranged at apart from reactor top porcelain ball is 800mm.The mixing material containing nitric acid, water and methyl alcohol of oxidative esterification tower tower reactor being discharged and the mist containing NO pass into above-mentioned trickle bed reactor respectively, and be 85 DEG C in reaction temperature, reaction pressure is 0.5MPa, and liquid hourly space velocity (LHSV) is 1h
-1, the mol ratio of NO and nitric acid is the generation methyl nitrite that reacts under the condition of 5, and the conversion ratio of nitric acid is 98.5%.
[embodiment 3]
By Fig. 1, Fig. 2, Fig. 3-1, Fig. 3-2, Fig. 3-3 and Fig. 3-4, the catalyst in trickle bed reactor adopts nickel catalyst, the gas passage pipe of the gas-liquid allotter in reactor and fluid passage pipe are equilateral triangle arrangement, and the percent opening of gas passage pipe on distribution grid is 30%, and the percent opening of fluid passage pipe on distribution grid is 50%, the short tube of fluid passage pipe accounts for 3% of described vertical short tube total length in the part above distribution grid, short tube lower end to stretch out below distribution grid 1000 millimeters, the short tubular portions be positioned at below distribution grid circumferentially evenly has aperture, the diameter d of aperture is 8mm, in foraminate gross area S1 and fluid passage pipe the ratio of sectional area S2 be 0.95:1, the stream breaker center be connected with short tube end have circular aperture 1, circumferentially equally distributed rectangular opening 6, the percent opening of the broken discharge orifice on stream breaker is 40%, the distance that gas-liquid allotter is arranged at apart from reactor top porcelain ball is 1200mm.The mixing material containing nitric acid, water and methyl alcohol of oxidative esterification tower tower reactor being discharged and the mist containing NO pass into above-mentioned trickle bed reactor respectively, and be 95 DEG C in reaction temperature, reaction pressure is 0.8MPa, and liquid hourly space velocity (LHSV) is 8.0h
-1, the mol ratio of NO and nitric acid is the generation methyl nitrite that reacts under the condition of 4, and the conversion ratio of nitric acid is 97.6%.
[embodiment 4]
By Fig. 1, Fig. 2, Fig. 3-1, Fig. 3-2, Fig. 3-3 and Fig. 3-4, the catalyst in trickle bed reactor adopts nickel catalyst, the gas passage pipe of the gas-liquid allotter in reactor and fluid passage pipe are equilateral triangle arrangement, and the percent opening of gas passage pipe on distribution grid is 20%, and the percent opening of fluid passage pipe on distribution grid is 30%, the short tube of fluid passage pipe accounts for 5% of described vertical short tube total length in the part above distribution grid, short tube lower end to stretch out below distribution grid 800 millimeters, the short tubular portions be positioned at below distribution grid circumferentially evenly has aperture, the diameter d of aperture is 5mm, in foraminate gross area S1 and fluid passage pipe the ratio of sectional area S2 be 0.9:1, the stream breaker center be connected with short tube end have circular aperture 1, circumferentially equally distributed triangular apertures 4, the percent opening of the broken discharge orifice on stream breaker is 30%, the distance that gas-liquid allotter is arranged at apart from reactor top porcelain ball is 1000mm.The mixing material containing nitric acid, water and methyl alcohol of oxidative esterification tower tower reactor being discharged and the mist containing NO pass into above-mentioned trickle bed reactor respectively, and be 120 DEG C in reaction temperature, reaction pressure is 1.5MPa, and liquid hourly space velocity (LHSV) is 2.5h
-1, the mol ratio of NO and nitric acid is the generation methyl nitrite that reacts under the condition of 10, and the conversion ratio of nitric acid is 98.7%.
[embodiment 5]
By Fig. 1, Fig. 2, Fig. 3-1, Fig. 3-2, Fig. 3-3 and Fig. 3-4, the catalyst in trickle bed reactor adopts nickel catalyst, the gas passage pipe of the gas-liquid allotter in reactor and fluid passage pipe are equilateral triangle arrangement, and the percent opening of gas passage pipe on distribution grid is 15%, and the percent opening of fluid passage pipe on distribution grid is 25%, the short tube of fluid passage pipe accounts for 12% of described vertical short tube total length in the part above distribution grid, short tube lower end to stretch out below distribution grid 600 millimeters, the short tubular portions be positioned at below distribution grid circumferentially evenly has aperture, the diameter d of aperture is 4mm, in foraminate gross area S1 and fluid passage pipe the ratio of sectional area S2 be 1:1, the stream breaker center be connected with short tube end have circular aperture 1, circumferentially equally distributed triangular apertures 5, the percent opening of the broken discharge orifice on stream breaker is 25%, the distance that gas-liquid allotter is arranged at apart from reactor top porcelain ball is 850mm.The mixing material containing nitric acid, water and methyl alcohol of oxidative esterification tower tower reactor being discharged and the mist containing NO pass into above-mentioned trickle bed reactor respectively, and be 100 DEG C in reaction temperature, reaction pressure is 1.0MPa, and liquid hourly space velocity (LHSV) is 4h
-1, the mol ratio of NO and nitric acid is the generation methyl nitrite that reacts under the condition of 6, and the conversion ratio of nitric acid is 99.1%.
[comparative example 1]
Adopt according to document CN200710039071.2[embodiment 1] in the gas-liquid allotter form that adopts, adopt the raw material identical with in the present invention's [embodiment 5], reaction condition, implementation step to carry out methyl nitrite production, nitric acid conversion ratio is 92%.
Claims (10)
1. a trickle bed reactor, comprises housing, gas pre-distributor, liquid pre-distributor, gas-liquid allotter, gas-phase product outlet and liquid product outlet;
Described gas-liquid allotter comprises distribution grid, gas passage pipe and fluid passage pipe;
Described gas passage pipe comprises circular cone top cover and upright short tube; The space that supplied gas passes in and out is formed between the upper end of described circular cone top cover and described upright short tube; The lower end of described upright short tube is arranged on described distribution grid;
Described fluid passage pipe is vertical short tube, and described vertical short tube runs through described distribution grid; Be positioned at vertical short tubular portions below described distribution grid and evenly have aperture alternately on the cross section of diverse location vertically;
Described gas passage pipe is uniformly distributed between described fluid passage pipe;
It is characterized in that, described vertical short tube is positioned at the part below described distribution grid, and its end is connected with stream breaker; Described stream breaker comprises the circular hole of center, and circumferentially equally distributed divergent shape bar stitches.
2. trickle bed reactor according to claim 1, is characterized in that, the divergent shape bar seam on described stream breaker is rectangle or triangle.
3. trickle bed reactor according to claim 1, is characterized in that, the divergent shape bar on described stream breaker is sewed with 3 ~ 6.
4. trickle bed reactor according to claim 1, is characterized in that, the rate of cracking of the divergent shape bar seam on described stream breaker is 10 ~ 40%.
5. trickle bed reactor according to claim 1, is characterized in that, the described vertical short tube part be positioned at above described distribution grid accounts for 3 ~ 20% of described vertical short tube total length.
6. trickle bed reactor according to claim 1, is characterized in that, the described vertical short tube part be positioned at below described distribution grid is 200 ~ 1000 millimeters.
7. trickle bed reactor according to claim 1, is characterized in that, the percent opening of described gas passage pipe on described distribution grid is 10 ~ 30%; The percent opening of described fluid passage pipe on described distribution grid is 10 ~ 50%.
8. trickle bed reactor according to claim 1, is characterized in that, the gas passage pipe on described distribution grid and fluid passage pipe are equilateral triangle arrangement.
9. trickle bed reactor according to claim 1, is characterized in that, the diameter d of described aperture is 3 ~ 8mm, in foraminate gross area S1 and fluid passage pipe the ratio of sectional area S2 be (0.75:1) ~ (1:1).
10. trickle bed reactor according to claim 1, it is characterized in that, described gas pre-distributor is arranged at described reactor head, described liquid pre-distributor is arranged at housing side surface upper part, described gas-phase product outlet is arranged at case side basifacial, and described liquid product outlet is arranged at described reactor bottom.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520786158.6U CN205127915U (en) | 2015-10-12 | 2015-10-12 | Trickle bed reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520786158.6U CN205127915U (en) | 2015-10-12 | 2015-10-12 | Trickle bed reactor |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN205127915U true CN205127915U (en) | 2016-04-06 |
Family
ID=55613741
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201520786158.6U Active CN205127915U (en) | 2015-10-12 | 2015-10-12 | Trickle bed reactor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN205127915U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113304696A (en) * | 2021-06-04 | 2021-08-27 | 东营海瑞宝新材料有限公司 | Diethyl toluene diamine synthesis device and synthesis process thereof |
-
2015
- 2015-10-12 CN CN201520786158.6U patent/CN205127915U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113304696A (en) * | 2021-06-04 | 2021-08-27 | 东营海瑞宝新材料有限公司 | Diethyl toluene diamine synthesis device and synthesis process thereof |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101279229B (en) | Trickle bed reactor | |
| CN101279228B (en) | Gas-liquid distributor of trickle bed reactor | |
| CN109985570A (en) | It is a kind of with subtracting the hydrogenator for rushing element | |
| CN205127915U (en) | Trickle bed reactor | |
| CN105642198A (en) | Fixed bed multiphase atomizing nozzle | |
| CN2834690Y (en) | Co-current gas-liquid distributor | |
| CN106000240A (en) | Cold hydrogen tank for hydrogenation reactor | |
| CN201959778U (en) | Gas-liquid separator | |
| CN2355786Y (en) | Gas-liquid distributor | |
| CN205288346U (en) | Gas -liquid distributor | |
| CN205235933U (en) | Trickle bed reaction subassembly | |
| CN108514854A (en) | A kind of circulation flow reactor of adipic dinitrile hydrogenation production hexamethylene diamine | |
| CN106799194A (en) | Gas-liquid allotter | |
| CN106563394A (en) | Gas-liquid distributor, trickle-bed reactor and gas-liquid reaction method | |
| CN214106875U (en) | Trickle bed reactor | |
| CN205650176U (en) | Heterogeneous atomizing nozzle of fixed bed | |
| CN202015610U (en) | Inlet diffuser of hydrogenation reactor | |
| CN204724142U (en) | A kind of suction overflow type gas-liquid allotter | |
| CN205216811U (en) | Gas -liquid separator | |
| CN110251982B (en) | High-operation-elasticity liquid distribution device and method | |
| CN201493099U (en) | Cooling hydrogen spraying pan | |
| CN201493097U (en) | Spiral grooved gas-liquid distributor | |
| CN215586003U (en) | Conversion gas mixing tower | |
| CN207929181U (en) | A kind of gas-liquid distributed architecture of big operating flexibility gas-liquid gas-solids reactors | |
| CN111558343A (en) | Gas-liquid mixing distribution system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |