CN112791671A - Heat exchange medium uniform distribution device of U-shaped tube organosilicon fluidized bed reactor - Google Patents
Heat exchange medium uniform distribution device of U-shaped tube organosilicon fluidized bed reactor Download PDFInfo
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- CN112791671A CN112791671A CN202011435726.XA CN202011435726A CN112791671A CN 112791671 A CN112791671 A CN 112791671A CN 202011435726 A CN202011435726 A CN 202011435726A CN 112791671 A CN112791671 A CN 112791671A
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- heat exchange
- exchange medium
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- 238000009827 uniform distribution Methods 0.000 title claims abstract description 13
- 238000009826 distribution Methods 0.000 claims abstract description 49
- 230000000712 assembly Effects 0.000 claims abstract description 8
- 238000000429 assembly Methods 0.000 claims abstract description 8
- 238000012423 maintenance Methods 0.000 abstract description 3
- NEHMKBQYUWJMIP-UHFFFAOYSA-N chloromethane Chemical compound ClC NEHMKBQYUWJMIP-UHFFFAOYSA-N 0.000 description 24
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 10
- 238000006243 chemical reaction Methods 0.000 description 10
- 239000000178 monomer Substances 0.000 description 9
- 229940050176 methyl chloride Drugs 0.000 description 8
- 239000011863 silicon-based powder Substances 0.000 description 7
- 239000003921 oil Substances 0.000 description 6
- 238000000034 method Methods 0.000 description 5
- 239000002245 particle Substances 0.000 description 4
- 229910052710 silicon Inorganic materials 0.000 description 4
- 239000010703 silicon Substances 0.000 description 4
- 230000000694 effects Effects 0.000 description 3
- 238000005243 fluidization Methods 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- 238000007086 side reaction Methods 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
- 239000012530 fluid Substances 0.000 description 2
- 230000008676 import Effects 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 1
- 238000000605 extraction 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
- 238000002791 soaking 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
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Abstract
The heat exchange medium uniform distribution device of the U-shaped tube organosilicon fluidized bed reactor comprises a jacket pre-distributor and a plurality of sets of heat exchange assemblies, wherein each set of heat exchange assembly comprises a heat exchange medium inlet branch tube, a heat exchange medium outlet branch tube and a plurality of sets of U-shaped heat exchange tubes, and the inlet and the outlet of each set of U-shaped heat exchange tubes are respectively communicated with the heat exchange medium inlet branch tube and the heat exchange medium outlet branch tube; 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. The invention can uniformly distribute heat exchange media, and ensure the stability and balance of 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 invention belongs to the field of chemical reaction equipment, relates to performance improvement of a heat exchange structure, and particularly relates to a uniform heat exchange medium distribution device of a U-shaped tube organosilicon fluidized bed reactor.
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, due to the stirring of bubbles and the rapid flow of particles, the heat transfer coefficient between the bed layer and the inner immersed heat exchange surface is high, and the heat exchange of the strong heat exchange reaction is greatly facilitated.
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 with a single tube structure mainly adopts a U-shaped tube, for example, the invention patent 201420388526.7 discloses an organosilicon fluidized bed reactor adopting the U-shaped tube for heat exchange, 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 in pipeline arrangement, operation and equipment maintenance is high; the novel organic silicon fluidized bed reactor developed in the invention patent 201821792172.7 strengthens gas distribution and heat conduction oil distribution, but the heat exchange liquid box is arranged at the top of the equipment, so that the equipment is difficult to overhaul, and potential safety hazards exist.
Disclosure of Invention
The invention provides a uniform heat exchange medium distribution device of a U-shaped tube organosilicon fluidized bed reactor, which is used for solving the problems of uneven heat exchange medium distribution, high investment and operation cost and the like in the prior art.
In order to realize the purpose of the invention, the following technical scheme is adopted:
the heat exchange medium uniform distribution device of the U-shaped tube organosilicon fluidized bed reactor comprises a jacket pre-distributor and a plurality of sets of heat exchange assemblies, wherein each set of heat exchange assembly comprises a heat exchange medium inlet branch tube, a heat exchange medium outlet branch tube and a plurality of sets of U-shaped heat exchange tubes, and the inlet and the outlet of each set of U-shaped heat exchange tubes are respectively communicated with the heat exchange medium inlet branch tube and the heat exchange medium outlet branch tube; 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.
When the heat exchange device works, a heat exchange medium enters the inlet distribution section of the jacket pre-distributor from the heat exchange medium inlet, then enters the U-shaped heat exchange tube after being distributed through the heat exchange medium inlet branch tube, is gathered to the heat exchange medium outlet branch tube after heat exchange, then enters the outlet distribution section of the jacket pre-distributor and leaves the reactor from the heat exchange medium outlet. Therefore, gas can directly flow through the reactor from the bottom, so that the non-ideal flows such as bias flow, dead zones and the like are inhibited, and the bulk fluidization effect of the fluidized bed reactor is improved; the heat exchange medium can be uniformly distributed to the U-shaped heat exchange tubes, so that the temperature distribution in the bed is uniform, the side reaction is inhibited, and the selectivity and the yield of the target product are improved.
In order to further realize the purpose of the invention, the following technical scheme can be adopted:
according to the heat exchange medium uniform distribution device of the U-shaped tube organosilicon fluidized bed reactor, the jacket pre-distributor is arranged on the outer side of the cylinder of the fluidized bed reactor, and the inlet distribution section and the outlet distribution section are annular cavities which are buckled relatively.
According to the heat exchange medium uniform distribution device of the U-shaped tube organosilicon fluidized bed reactor, each set of heat exchange component is provided with the heat exchange medium inlet branch tube and the heat exchange medium outlet branch tube in parallel, one end of each of the heat exchange medium inlet branch tube and the heat exchange medium outlet branch tube is fixedly connected with the inlet distribution section and the outlet distribution section respectively, and the other end of each of the heat exchange medium inlet branch tube and the heat exchange medium outlet branch tube is sealed.
According to the heat exchange medium uniform distribution device of the U-shaped tube organosilicon fluidized bed reactor, the distance between the heat exchange medium inlet branch pipe and the heat exchange medium outlet branch pipe can be adjusted.
The heat exchange medium uniform distribution device of the U-shaped tube organosilicon fluidized bed reactor is characterized in that medium flow openings are formed in the bottoms and/or the side surfaces of the heat exchange medium inlet branch tube and the heat exchange medium outlet branch tube, and the medium flow openings are matched with the inlet and the outlet of the U-shaped heat exchange tube.
According to the heat exchange medium uniform distribution device of the U-shaped tube organosilicon fluidized bed reactor, more than 3 sets of heat exchange components are arranged.
Compared with the prior art, the invention has the advantages that:
the invention can ensure that heat exchange media are uniformly distributed, maximally increase the heat exchange area by utilizing the U-shaped heat exchange tube, facilitate the timely and uniform extraction of reaction heat, ensure the stability and balance of temperature distribution in the fluidized bed, improve the yield of organosilicon monomers and inhibit side reactions.
The invention has reasonable structure, stable working performance, convenient arrangement and maintenance of equipment and pipelines and safe operation and use.
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 view 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 technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the 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, in the heat exchange medium uniform distribution device of the U-shaped tube organosilicon fluidized bed reactor disclosed in this embodiment, the fluidized bed reactor is a sealed cylinder 1 with a cavity inside, a silicon powder inlet 11 is formed at the bottom of the cylinder 1, a coarse 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 transfer 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.
In the working process of the embodiment, silicon powder enters the barrel body 1 from the silicon powder inlet 11 and the inner extension pipe 17, chloromethane gas enters the barrel body 1 from the chloromethane gas inlet 12 through the inverted cone-shaped distributor, reacts with the silicon powder under the action of a catalyst to generate an organosilicon crude monomer and emit a large amount of heat, and the organosilicon crude monomer generated by the reaction and unreacted chloromethane gas pass through the heat exchange component at the upper part and leave the barrel body 1 from the crude monomer gas-phase outlet 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 (6)
1. The uniform heat exchange medium distribution device of the U-shaped tube organosilicon fluidized bed reactor is characterized by comprising a jacket pre-distributor and a plurality of sets of heat exchange assemblies, wherein each set of heat exchange assembly comprises a heat exchange medium inlet branch tube, a heat exchange medium outlet branch tube and a plurality of sets of U-shaped heat exchange tubes, and the inlet and the outlet of each set of U-shaped heat exchange tubes are respectively communicated with the heat exchange medium inlet branch tube and the heat exchange medium outlet branch tube; 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 device for uniformly distributing heat exchange media of the U-shaped tube organosilicon fluidized bed reactor as claimed in claim 1, wherein the jacket pre-distributor is installed outside the cylinder of the fluidized bed reactor, and the inlet distribution section and the outlet distribution section are annular cavities which are buckled relatively.
3. The device for uniformly distributing heat exchange media of a U-shaped tube organosilicon fluidized bed reactor as claimed in 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 device for uniformly distributing heat exchange medium of a U-shaped tube organosilicon fluidized bed reactor as claimed in claim 1, wherein the distance between the heat exchange medium inlet branch tube and the heat exchange medium outlet branch tube can be adjusted.
5. The heat exchange medium uniform distribution device of the U-shaped tube organosilicon fluidized bed reactor as claimed in claim 1, wherein the bottom and/or the side 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-shaped heat exchange tube.
6. The device for uniformly distributing heat exchange media of the U-shaped tube organosilicon fluidized bed reactor as claimed in claim 1, wherein more than 3 sets of heat exchange assemblies are arranged.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202011435726.XA CN112791671B (en) | 2020-12-10 | 2020-12-10 | Heat exchange medium uniform distribution device of U-shaped tube organosilicon fluidized bed reactor |
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| CN202011435726.XA CN112791671B (en) | 2020-12-10 | 2020-12-10 | Heat exchange medium uniform distribution device of U-shaped tube organosilicon fluidized bed reactor |
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| CN112791671B CN112791671B (en) | 2022-08-30 |
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Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN200939377Y (en) * | 2006-08-29 | 2007-08-29 | 闫慧光 | Organosilyl fluidized-bed reactor |
| CN101130551A (en) * | 2007-09-05 | 2008-02-27 | 青岛科技大学 | Conduction oil distributor of organosilicon monomer fluid bed reactor and method of manufacturing the same |
| CN101564665A (en) * | 2009-05-27 | 2009-10-28 | 江苏宏达新材料股份有限公司 | Fluidized bed reactor |
| CN201598184U (en) * | 2009-12-01 | 2010-10-06 | 倪云达 | Fluidized bed reactor capable of stabilizing reaction temperature in production of trichlorosilane |
| CN102744016A (en) * | 2012-06-21 | 2012-10-24 | 四川亚联高科技股份有限公司 | Novel methanol converter |
| CN205182683U (en) * | 2015-09-02 | 2016-04-27 | 德艾柯工程技术（上海）有限公司 | Novel board -like axial reactor |
| CA2965581A1 (en) * | 2017-04-28 | 2017-07-05 | Imperial Oil Resources Limited | Heat recovery from oil sand tailings utilizing a fluidized bed |
| CN109520329A (en) * | 2017-09-19 | 2019-03-26 | 浙江盾安机械有限公司 | Heat exchanger |
| CN209295766U (en) * | 2018-12-30 | 2019-08-23 | 张占山 | Detachable heat exchanger, reaction member and reactor |
-
2020
- 2020-12-10 CN CN202011435726.XA patent/CN112791671B/en active Active
Patent Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN200939377Y (en) * | 2006-08-29 | 2007-08-29 | 闫慧光 | Organosilyl fluidized-bed reactor |
| CN101130551A (en) * | 2007-09-05 | 2008-02-27 | 青岛科技大学 | Conduction oil distributor of organosilicon monomer fluid bed reactor and method of manufacturing the same |
| CN101564665A (en) * | 2009-05-27 | 2009-10-28 | 江苏宏达新材料股份有限公司 | Fluidized bed reactor |
| CN201598184U (en) * | 2009-12-01 | 2010-10-06 | 倪云达 | Fluidized bed reactor capable of stabilizing reaction temperature in production of trichlorosilane |
| CN102744016A (en) * | 2012-06-21 | 2012-10-24 | 四川亚联高科技股份有限公司 | Novel methanol converter |
| CN205182683U (en) * | 2015-09-02 | 2016-04-27 | 德艾柯工程技术（上海）有限公司 | Novel board -like axial reactor |
| CA2965581A1 (en) * | 2017-04-28 | 2017-07-05 | Imperial Oil Resources Limited | Heat recovery from oil sand tailings utilizing a fluidized bed |
| CN109520329A (en) * | 2017-09-19 | 2019-03-26 | 浙江盾安机械有限公司 | Heat exchanger |
| CN209295766U (en) * | 2018-12-30 | 2019-08-23 | 张占山 | Detachable heat exchanger, reaction member and reactor |
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