CN214598927U - U-shaped tube organosilicon fluidized bed reactor with uniformly distributed heat exchange medium - Google Patents
U-shaped tube organosilicon fluidized bed reactor with uniformly distributed heat exchange medium Download PDFInfo
- Publication number
- CN214598927U CN214598927U CN202022992425.9U CN202022992425U CN214598927U CN 214598927 U CN214598927 U CN 214598927U CN 202022992425 U CN202022992425 U CN 202022992425U CN 214598927 U CN214598927 U CN 214598927U
- Authority
- CN
- China
- Prior art keywords
- heat exchange
- exchange medium
- inlet
- outlet
- tube
- 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
- NEHMKBQYUWJMIP-UHFFFAOYSA-N chloromethane Chemical compound ClC NEHMKBQYUWJMIP-UHFFFAOYSA-N 0.000 claims abstract description 48
- 238000009826 distribution Methods 0.000 claims abstract description 42
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 claims abstract description 12
- 239000000178 monomer Substances 0.000 claims abstract description 12
- 239000011863 silicon-based powder Substances 0.000 claims abstract description 9
- 229940050176 methyl chloride Drugs 0.000 claims description 21
- 230000000712 assembly Effects 0.000 claims description 6
- 238000000429 assembly Methods 0.000 claims description 6
- 238000012423 maintenance Methods 0.000 abstract description 3
- 238000006243 chemical reaction Methods 0.000 description 10
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 6
- 239000003921 oil Substances 0.000 description 6
- 230000000694 effects Effects 0.000 description 4
- 238000005243 fluidization Methods 0.000 description 4
- 230000008676 import Effects 0.000 description 4
- 238000000034 method Methods 0.000 description 4
- 239000002245 particle Substances 0.000 description 4
- 229910052710 silicon Inorganic materials 0.000 description 4
- 239000010703 silicon Substances 0.000 description 4
- 235000013312 flour Nutrition 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 239000000377 silicon dioxide Substances 0.000 description 3
- 230000009471 action Effects 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000002349 favourable effect Effects 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 238000007086 side reaction Methods 0.000 description 2
- 238000002791 soaking Methods 0.000 description 2
- 238000009827 uniform distribution Methods 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 230000002401 inhibitory effect Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
- 238000006276 transfer reaction Methods 0.000 description 1
- 230000003245 working effect Effects 0.000 description 1
Images
Landscapes
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The U-shaped tube organosilicon fluidized bed reactor with uniformly distributed heat exchange media comprises a cylinder body with a silicon powder inlet, a crude monomer gas phase outlet, a chloromethane gas inlet, a heat exchange medium inlet and a heat exchange medium outlet, wherein a jacket pre-distributor is arranged at the upper part of the cylinder body, and a plurality of sets of heat exchange components are arranged in the cylinder body; each set of heat exchange assembly comprises a heat exchange medium inlet branch pipe, a heat exchange medium outlet branch pipe and a plurality of groups of U-shaped heat exchange pipes, wherein the inlet and the outlet of each group of U-shaped heat exchange pipes are respectively communicated with the heat exchange medium inlet branch pipe and the heat exchange medium outlet branch pipe; the jacket pre-distributor comprises an inlet distribution section and an outlet distribution section, wherein the inlet distribution section is respectively communicated with the heat exchange medium inlet and the heat exchange medium inlet branch pipe, and the outlet distribution section is respectively communicated with the heat exchange medium outlet and the heat exchange medium outlet branch pipe. The utility model can uniformly distribute the heat exchange medium, and ensure the stability and balance of the temperature distribution in the fluidized bed; reasonable structure, stable working performance, convenient equipment and pipeline arrangement and maintenance, and safe operation and use.
Description
Technical Field
The utility model belongs to the chemical reaction equipment field relates to the performance improvement of heat transfer structure, specifically is a U type pipe organosilicon fluidized bed reactor of heat transfer medium equipartition.
Background
The fluidized bed is a device which drives solid particles to move like fluid by means of gas or liquid flow and simultaneously carries out reaction between the particles and the fluid, and is characterized in that the particles in the fluidized bed are in a moving state, and a bed layer in a container has an obvious interface, and the fluidized bed has a series of advantages of high heat transfer, mass transfer and chemical reaction rates, large operation flexibility, large production capacity, simple and compact structure and the like. Especially, because of the stirring of bubbles and the rapid flow of particles, the heat transfer coefficient between the bed layer and the inner soaking heat exchange surface is high, and the heat exchange of the strong heat exchange reaction is very favorable.
In the process of synthesizing the organic silicon monomer, chloromethane gas and silicon powder react violently under the action of a catalyst, a large amount of heat is released, the reaction heat is taken out timely and uniformly, the temperature distribution in the fluidized bed is kept stable and balanced, and the method has important effects of improving the yield of the organic silicon monomer and inhibiting side reactions.
The heat exchange tube bundle of the currently used organosilicon fluidized bed reactor mainly has two structures of a single tube type and a sleeve type. For example, in the 'organosilicon fluidized bed reactor' disclosed in patent 201010610050.3, the heat exchange tube bundle adopts a finger-shaped sleeve, but the arrangement of a heat transfer oil distribution device is unreasonable, so that the dilute phase section of the reactor is too high, which is not beneficial to reaction; the invention patent 201310319627.9 discloses a fluidized bed reactor and its application in producing organosilicon monomer, its heat exchange tube bundle also adopts the finger-type sleeve, the reactor can realize the uniform arrangement of the heat-conducting oil, but its gas phase outlet is set up in the side of reactor shell, cause the gas bias flow to be unfavorable for the scattered fluidization; the invention patent 200710145747.6 discloses a heat exchange tube bundle of a soaking straight-return type organosilicon fluidized bed reactor, which adopts a finger-shaped sleeve for heat exchange and can realize uniform distribution of heat-conducting oil and direct flow of gas. The sleeve structure is beneficial to scattered fluidization, but the diameter of the outer pipe of the heat exchange pipe is correspondingly increased due to the inner sleeve structure and the outer sleeve structure, so that the heat exchange area is small.
The heat exchange tube of the single tube structure mainly adopts a U-shaped tube, so the organosilicon fluidized bed reactor adopting the U-shaped tube for heat exchange disclosed in the novel patent 201420388526.7 is used for preventing caking, gas enters the reactor in two layers to improve the bulk fluidization effect, but the technology adopts external distribution for heat conduction oil distribution, large-scale equipment needs to be provided with more than 20 heat conduction oil inlets and outlets, and the difficulty of pipeline arrangement, operation and equipment maintenance is high; the utility model discloses a "a novel organosilicon fluidized bed reactor" of 201821792172.7 development has strengthened the distribution of gas distribution and conduction oil, but the heat transfer liquid case setting is at the equipment top, and organosilicon operation is intermittent type operation in addition, and the heat transfer liquid discharges the degree of difficulty when equipment intermittent type operation and maintenance big, increases equipment weight on the one hand, and on the other hand has the potential safety hazard.
SUMMERY OF THE UTILITY MODEL
The utility model provides a U type pipe organosilicon fluidized bed reactor of heat transfer medium equipartition for finger pipe heat transfer area that exists among the solution prior art is on the small side, U type pipe formula fluidization effect is poor, investment and operating cost scheduling problem.
In order to realize the utility model discloses an aim at, adopt following technical scheme:
the U-shaped tube organosilicon fluidized bed reactor with uniformly distributed heat exchange media comprises a cylinder body, wherein the bottom of the cylinder body is provided with a silicon powder inlet, the top of the cylinder body is provided with a coarse monomer gas phase outlet, the lower part of the cylinder body is provided with a methyl chloride gas inlet, the two sides of the upper part of the cylinder body are provided with a heat exchange medium inlet and a heat exchange medium outlet, the upper part of the cylinder body is provided with a jacket pre-distributor, and a plurality of sets of heat exchange assemblies are arranged in the cylinder body; each set of heat exchange assembly comprises a heat exchange medium inlet branch pipe, a heat exchange medium outlet branch pipe and a plurality of sets of U-shaped heat exchange pipes, wherein the inlet and the outlet of each set of U-shaped heat exchange pipe are respectively communicated with the heat exchange medium inlet branch pipe and the heat exchange medium outlet branch pipe; the jacket pre-distributor comprises an inlet distribution section and an outlet distribution section, the inlet distribution section is respectively communicated with the heat exchange medium inlet and the heat exchange medium inlet branch pipe, and the outlet distribution section is respectively communicated with the heat exchange medium outlet and the heat exchange medium outlet branch pipe.
In order to further realize the purpose of the utility model, the following technical scheme can also be adopted:
the U-shaped tube organosilicon fluidized bed reactor with the uniformly distributed heat exchange media is characterized in that the jacket pre-distributor is arranged on the outer side of the cylinder, and the inlet distribution section and the outlet distribution section are annular cavities which are buckled relatively.
In the U-tube organosilicon fluidized bed reactor with uniformly distributed heat exchange media, each set of heat exchange assembly has the heat exchange medium inlet branch tube and the heat exchange medium outlet branch tube arranged in parallel, one end of each of the heat exchange medium inlet branch tube and the heat exchange medium outlet branch tube is respectively connected and fixed with the inlet distribution section and the outlet distribution section, and the other end of each of the heat exchange medium inlet branch tube and the heat exchange medium outlet branch tube is sealed.
Further, according to the U-shaped tube organosilicon fluidized bed reactor with the uniformly distributed heat exchange medium, the distance between the heat exchange medium inlet branch pipe and the heat exchange medium outlet branch pipe can be adjusted.
According to the U-shaped tube organic silicon fluidized bed reactor with the uniformly distributed heat exchange media, the bottom and/or the side surface of the heat exchange medium inlet branch tube and the heat exchange medium outlet branch tube are/is provided with the medium flow ports, and the medium flow ports are matched with the inlet and the outlet of the U-shaped heat exchange tube.
The U-shaped tube organosilicon fluidized bed reactor with the uniformly distributed heat exchange medium is characterized in that a methyl chloride gas distributor fixed on the inner wall of the cylinder body is arranged between the methyl chloride gas inlet and the bottom of the heat exchange component, the silicon powder inlet is provided with the inner extension tube, and the upper end of the inner extension tube penetrates through the methyl chloride gas distributor.
Further, the methyl chloride gas distributor is an inverted cone-shaped distributor, and the taper of the methyl chloride gas distributor is 60-180 degrees.
The U-shaped tube organosilicon fluidized bed reactor with the uniformly distributed heat exchange media is characterized in that more than 3 sets of heat exchange components are arranged in the cylinder body.
Compared with the prior art, the utility model has the advantages of:
the utility model discloses can guarantee that heat transfer medium is evenly arranged, utilize the increase heat transfer area of U type heat exchange tube maximize, be favorable to the reaction heat in time, evenly take out, guarantee in the fluidized bed temperature distribution's stability and equilibrium, improve organosilicon monomer yield, restrain the side reaction.
The utility model discloses rational in infrastructure, working property are stable, make things convenient for equipment, pipeline to arrange and overhaul, operation safety in utilization.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below.
Fig. 1 is a schematic structural diagram of the present invention;
FIG. 2 is a schematic diagram of the jacket predistributor and heat exchange assembly of FIG. 1;
fig. 3 is a schematic structural view of the U-shaped heat exchange tube in fig. 1.
Reference numerals: 1-cylinder, 11-silicon powder inlet, 12-chloromethane gas inlet, 13-heat exchange medium outlet, 14-heat exchange medium inlet, 15-crude monomer gas phase outlet, 16-chloromethane gas distributor and 17-inner extension pipe; 21-inlet distribution section, 22-outlet distribution section; 3-heat exchange medium outlet branch pipe, 31-first outlet branch pipe, 32-second outlet branch pipe, 33-third outlet branch pipe, 34-fourth outlet branch pipe, 35-fifth outlet branch pipe; 4-heat exchange medium inlet branch pipe, 41-first inlet branch pipe, 42-second inlet branch pipe, 43-third inlet branch pipe, 44-fourth inlet branch pipe and 45-fifth inlet branch pipe; 5-U type heat exchange tube.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are some, but not all, embodiments of the present invention.
As shown in fig. 1-3, the U-tube organosilicon fluidized bed reactor with uniformly distributed heat exchange media disclosed in this embodiment is shaped as a sealed cylinder 1 with a cavity inside, a silicon powder inlet 11 is formed at the bottom of the cylinder 1, a crude monomer gas phase outlet 15 is formed at the top, a methyl chloride gas inlet 12 is formed at the lower part, and a heat exchange medium inlet 14 and a heat exchange medium outlet 13 are formed at both sides of the upper part; the upper part of the cylinder body 1 is provided with a jacket pre-distributor, and a plurality of sets of heat exchange assemblies are arranged in the cylinder body 1.
The heat exchange assembly in this embodiment is provided with 5 sets, sets up many sets of heat exchange assemblies and increases heat transfer area simultaneously also can be better carry out evenly distributed with heat transfer medium, absorbs the heat that releases when methyl chloride gas reacts with silicon, in time, evenly takes out the reaction heat to and keep the stability and the equilibrium of temperature distribution in the fluidized bed.
As shown in fig. 2 and 3, each set of heat exchange assembly in this embodiment includes a heat exchange medium inlet branch pipe 4, a heat exchange medium outlet branch pipe 3, and a plurality of U-shaped heat exchange pipes, and an inlet and an outlet of each U-shaped heat exchange pipe 5 are respectively communicated with the heat exchange medium inlet branch pipe 4 and the heat exchange medium outlet branch pipe 3. The heat exchange medium outlet branch pipes 3 of the 5 sets of heat exchange assemblies are respectively a first outlet branch pipe 31, a second outlet branch pipe 32, a third outlet branch pipe 33, a fourth outlet branch pipe 34 and a fifth outlet branch pipe 35; the heat exchange medium inlet branch pipes 4 corresponding to the heat exchange medium inlet branch pipes are respectively a first inlet branch pipe 41, a second inlet branch pipe 42, a third inlet branch pipe 43, a fourth inlet branch pipe 44 and a fifth inlet branch pipe 45.
The heat exchange medium inlet branch pipe 4 and the heat exchange medium outlet branch pipe 3 are distributed in parallel and are used as a support beam to fix and support the U-shaped heat exchange pipe 5; and secondly, the uniform distribution of heat exchange media in the U-shaped heat exchange tubes 5 is realized. Because barrel 1 is mostly circular structure, for the maximize and the rational arrangement that realize U type heat exchange tube 5 quantity, heat transfer medium import branch pipe 4, heat transfer medium export branch pipe 3 quantity are corresponding, and each heat transfer medium import branch pipe 4, heat transfer medium export branch pipe 3 adopt to stagger to arrange in many sets of heat exchange assemblies simultaneously to guarantee heat transfer medium's heat absorption effect.
The heat exchange medium inlet branch pipe 4 and the heat exchange medium outlet branch pipe 3 in each set of heat exchange assembly are arranged in parallel on the cross section of the cylinder body 1, one end of each of the heat exchange medium inlet branch pipe 4 and the heat exchange medium outlet branch pipe 3 is fixedly connected with the inlet distribution section 21 and the outlet distribution section 22 respectively, and the other end of each of the heat exchange medium inlet branch pipe 4 and the heat exchange medium outlet branch pipe 3 is closed. The distance between the heat exchange medium inlet branch pipe 4 and the heat exchange medium outlet branch pipe 3 can be adjusted. The bottom and/or the side surface of the heat exchange medium inlet branch pipe 4 and the heat exchange medium outlet branch pipe 3 are/is provided with medium flow openings, and the medium flow openings are matched with the inlet and the outlet of the U-shaped heat exchange pipe 5.
With continued reference to fig. 2, the jacket predistributor of the present embodiment is installed outside the upper portion of the cylinder 1, and includes an inlet distribution section 21 and an outlet distribution section 22, the inlet distribution section 21 is respectively communicated with the heat exchange medium inlet 14 and the heat exchange medium inlet branch pipe 4, and the outlet distribution section 22 is respectively communicated with the heat exchange medium outlet 13 and the heat exchange medium outlet branch pipe 3; the inlet distribution section 21 and the outlet distribution section 22 are annular cavities which are buckled relatively.
In order to adjust and control the methyl chloride gas entering the cylinder body 1, a methyl chloride gas distributor 16 fixed on the inner wall of the cylinder body 1 is arranged between the methyl chloride gas inlet 12 and the bottom of the heat exchange component, meanwhile, an inner extension pipe 17 is arranged at the silicon powder inlet 11, and the upper end of the inner extension pipe 17 penetrates through the methyl chloride gas distributor 16.
As shown in fig. 1, the methyl chloride gas distributor 16 in this embodiment is an inverted cone distributor, the taper is 120 °, and the taper can be selected from 60 ° to 180 ° according to the requirement and the flow rate of the methyl chloride gas.
The utility model discloses during operation, silica flour gets into barrel 1 by silica flour import 11, interior extension pipe 17, and methyl chloride gas gets into barrel 1 through the back taper distributor from methyl chloride gas import 12, reacts with silica flour under the catalyst action and generates the crude monomer of organosilicon, and emits a large amount of heats, and the crude monomer of organosilicon that the reaction generated and unreacted methyl chloride gas pass the heat transfer subassembly on upper portion, leave barrel 1 by crude monomer gas phase export 15; the heat exchange medium enters the inlet distribution section 21 of the jacket pre-distributor from the heat exchange medium inlet 14, is distributed to the heat exchange medium inlet branch pipe 4, then enters the U-shaped heat exchange pipe 5, is converged to the heat exchange medium outlet branch pipe 3 after heat exchange, enters the outlet distribution section 22 on the other side, and leaves the barrel 1 through the heat exchange medium outlet 13.
The heat exchange medium flows from the top to the bottom of the U-shaped heat exchange tube 5, flows reversely to the top after reaching the U-shaped bend at the bottom, and absorbs heat in the flowing process, so that the reaction heat is timely and uniformly taken out, and the stability and the balance of the temperature distribution in the fluidized bed are kept.
The technical contents not described in detail in the present invention are all known techniques.
Claims (8)
1. The U-shaped tube organosilicon fluidized bed reactor with uniformly distributed heat exchange media comprises a cylinder body and is characterized in that the bottom of the cylinder body is provided with a silicon powder inlet, the top of the cylinder body is provided with a crude monomer gas phase outlet, the lower part of the cylinder body is provided with a chloromethane gas inlet, the two sides of the upper part of the cylinder body are provided with a heat exchange medium inlet and a heat exchange medium outlet, the upper part of the cylinder body is provided with a jacket pre-distributor, and a plurality of sets of heat exchange assemblies are arranged in the cylinder body; each set of heat exchange assembly comprises a heat exchange medium inlet branch pipe, a heat exchange medium outlet branch pipe and a plurality of sets of U-shaped heat exchange pipes, wherein the inlet and the outlet of each set of U-shaped heat exchange pipe are respectively communicated with the heat exchange medium inlet branch pipe and the heat exchange medium outlet branch pipe; the jacket pre-distributor comprises an inlet distribution section and an outlet distribution section, the inlet distribution section is respectively communicated with the heat exchange medium inlet and the heat exchange medium inlet branch pipe, and the outlet distribution section is respectively communicated with the heat exchange medium outlet and the heat exchange medium outlet branch pipe.
2. The U-tube organosilicon fluidized bed reactor with uniformly distributed heat exchange media according to claim 1, wherein the jacket pre-distributor is installed outside the cylinder, and the inlet distribution section and the outlet distribution section are annular cavities which are buckled relatively.
3. The U-tube organosilicon fluidized bed reactor with uniformly distributed heat exchange media according to claim 1, wherein the heat exchange medium inlet branch tube and the heat exchange medium outlet branch tube in each set of heat exchange assembly are arranged in parallel, one end of the heat exchange medium inlet branch tube and one end of the heat exchange medium outlet branch tube are respectively connected and fixed with the inlet distribution section and the outlet distribution section, and the other end of the heat exchange medium inlet branch tube and the other end of the heat exchange medium outlet branch tube are closed.
4. The U-tube organosilicon fluidized bed reactor with uniformly distributed heat exchange media of claim 3, wherein the distance between the heat exchange medium inlet branch tube and the heat exchange medium outlet branch tube can be adjusted.
5. The U-tube organosilicon fluidized bed reactor with uniformly distributed heat exchange media according to claim 1, wherein the bottoms and/or sides of the heat exchange medium inlet branch tube and the heat exchange medium outlet branch tube are/is provided with medium flow ports, and the medium flow ports are matched with the inlet and the outlet of the U-tube heat exchange tube.
6. The U-tube organosilicon fluidized bed reactor with uniformly distributed heat exchange media according to claim 1, wherein a methyl chloride gas distributor fixed on the inner wall of the cylinder body is arranged between the methyl chloride gas inlet and the bottom of the heat exchange component, the silicon powder inlet is provided with an inner extension tube, and the upper end of the inner extension tube passes through the methyl chloride gas distributor.
7. The U-tube organosilicon fluidized bed reactor with uniformly distributed heat exchange media according to claim 6, wherein the methyl chloride gas distributor is an inverted cone distributor with the taper of 60-180 °.
8. The organosilicon fluidized bed reactor with U-shaped tubes and uniformly distributed heat exchange media as claimed in claim 1, wherein more than 3 sets of heat exchange components are arranged in the cylinder.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202022992425.9U CN214598927U (en) | 2020-12-10 | 2020-12-10 | U-shaped tube organosilicon fluidized bed reactor with uniformly distributed heat exchange medium |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202022992425.9U CN214598927U (en) | 2020-12-10 | 2020-12-10 | U-shaped tube organosilicon fluidized bed reactor with uniformly distributed heat exchange medium |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN214598927U true CN214598927U (en) | 2021-11-05 |
Family
ID=78430024
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202022992425.9U Active CN214598927U (en) | 2020-12-10 | 2020-12-10 | U-shaped tube organosilicon fluidized bed reactor with uniformly distributed heat exchange medium |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN214598927U (en) |
-
2020
- 2020-12-10 CN CN202022992425.9U patent/CN214598927U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN100512941C (en) | Slurry bubble columun reactor having internal circulation and external heat-exchanging and the application | |
| CN103240036B (en) | A kind of heat transfer reactor of Anti-temperature difference stress and combinations thereof device and application | |
| CN103341341B (en) | One prepares butadiene fluidized-bed reactor | |
| CN102274707A (en) | Slurry reactor used for producing liquid fuel | |
| CN103111239B (en) | A kind of air cooling methanol reactor | |
| CN109850918A (en) | A kind of reactors for synthesis of ammonia and technique | |
| CN103446957B (en) | The fasten cold hydrogen case of flow that a kind of cold hydrogen advances | |
| CN214598927U (en) | U-shaped tube organosilicon fluidized bed reactor with uniformly distributed heat exchange medium | |
| Li et al. | Waste minimization and efficient disposal of particles in optimized organic silicon production | |
| CN214681643U (en) | Tubular organosilicon fluidized bed reactor with uniformly distributed heat exchange medium | |
| CN102212080A (en) | Reaction device for preparing methyl chlorosilane and reaction system comprising same | |
| CN112791671B (en) | Heat exchange medium uniform distribution device of U-shaped tube organosilicon fluidized bed reactor | |
| CN201240855Y (en) | Fluid bed reactor | |
| CN214681631U (en) | Anti-caking U-shaped tube organic silicon fluidized bed reactor | |
| CN104096519B (en) | Fluidized-bed reactor and its application | |
| CN208944112U (en) | A kind of adiponitrile cyanation device | |
| CN102205221B (en) | Fixed bed catalyst reactor having heat-exchange medium distributing and gathering structure | |
| CN101219920A (en) | Ethanol dehydration technique adopting molecular sieve catalyst | |
| CN2785674Y (en) | Raw material liquid evaporation device possessing liquid distributor mounted in fluid bed | |
| CN206604395U (en) | A kind of gas mixer produced for methacrylaldehyde | |
| CN201768553U (en) | Gas-phase synthesis dimethyl ether fluidized bed reactor | |
| CN202860502U (en) | Vertical type water-cooled tube reactor | |
| CN103285782B (en) | Catalyst tremie pipe | |
| CN204841626U (en) | Recycle and regeneration agent temperature controller | |
| CN205055980U (en) | Isothermal fixed bed reation kettle |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |