CN114653313A - Organosilicon fluidized bed reactor - Google Patents
Organosilicon fluidized bed reactor Download PDFInfo
- Publication number
- CN114653313A CN114653313A CN202210364540.2A CN202210364540A CN114653313A CN 114653313 A CN114653313 A CN 114653313A CN 202210364540 A CN202210364540 A CN 202210364540A CN 114653313 A CN114653313 A CN 114653313A
- Authority
- CN
- China
- Prior art keywords
- reactor
- oil
- cavity
- air
- fixedly connected
- 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.)
- Pending
Links
- 239000000463 material Substances 0.000 claims abstract description 110
- 238000006243 chemical reaction Methods 0.000 claims abstract description 77
- 238000003756 stirring Methods 0.000 claims abstract description 45
- 230000000694 effects Effects 0.000 claims abstract description 10
- 238000007789 sealing Methods 0.000 claims description 57
- YKTSYUJCYHOUJP-UHFFFAOYSA-N [O--].[Al+3].[Al+3].[O-][Si]([O-])([O-])[O-] Chemical compound [O--].[Al+3].[Al+3].[O-][Si]([O-])([O-])[O-] YKTSYUJCYHOUJP-UHFFFAOYSA-N 0.000 claims description 11
- 238000010438 heat treatment Methods 0.000 claims description 9
- 229910001220 stainless steel Inorganic materials 0.000 claims description 5
- 239000010935 stainless steel Substances 0.000 claims description 5
- 229920001296 polysiloxane Polymers 0.000 claims 9
- FBBDOOHMGLLEGJ-UHFFFAOYSA-N methane;hydrochloride Chemical compound C.Cl FBBDOOHMGLLEGJ-UHFFFAOYSA-N 0.000 claims 3
- 239000007789 gas Substances 0.000 abstract description 77
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 abstract description 15
- 239000010703 silicon Substances 0.000 abstract description 5
- 229910052710 silicon Inorganic materials 0.000 abstract description 5
- 239000012495 reaction gas Substances 0.000 abstract description 3
- 239000000203 mixture Substances 0.000 abstract 1
- 239000003921 oil Substances 0.000 description 281
- NEHMKBQYUWJMIP-UHFFFAOYSA-N chloromethane Chemical compound ClC NEHMKBQYUWJMIP-UHFFFAOYSA-N 0.000 description 48
- 238000000034 method Methods 0.000 description 34
- 230000008569 process Effects 0.000 description 32
- 229940050176 methyl chloride Drugs 0.000 description 22
- 230000009471 action Effects 0.000 description 13
- 239000000047 product Substances 0.000 description 12
- 230000005484 gravity Effects 0.000 description 10
- 239000011863 silicon-based powder Substances 0.000 description 10
- 238000001816 cooling Methods 0.000 description 8
- 230000036632 reaction speed Effects 0.000 description 8
- 230000007774 longterm Effects 0.000 description 5
- 239000002699 waste material Substances 0.000 description 5
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 4
- WCUXLLCKKVVCTQ-UHFFFAOYSA-M Potassium chloride Chemical compound [Cl-].[K+] WCUXLLCKKVVCTQ-UHFFFAOYSA-M 0.000 description 4
- 238000005299 abrasion Methods 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 238000002156 mixing Methods 0.000 description 4
- 230000009286 beneficial effect Effects 0.000 description 3
- 238000000746 purification Methods 0.000 description 3
- 150000003377 silicon compounds Chemical class 0.000 description 3
- 238000010521 absorption reaction Methods 0.000 description 2
- 230000001174 ascending effect Effects 0.000 description 2
- 238000007664 blowing Methods 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 238000013021 overheating Methods 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 235000011164 potassium chloride Nutrition 0.000 description 2
- 239000001103 potassium chloride Substances 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 239000000376 reactant Substances 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 239000002918 waste heat Substances 0.000 description 2
- 238000006555 catalytic reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 229910010272 inorganic material Inorganic materials 0.000 description 1
- 239000011147 inorganic material Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000000178 monomer Substances 0.000 description 1
- 239000011368 organic material Substances 0.000 description 1
- 238000004804 winding Methods 0.000 description 1
Images
Classifications
-
- 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
-
- 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
- B01J8/005—Separating solid material from the gas/liquid stream
- B01J8/006—Separating solid material from the gas/liquid stream by filtration
-
- 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
- B01J8/1818—Feeding of the fluidising gas
- B01J8/1827—Feeding of the fluidising gas the fluidising gas being a reactant
-
- 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
- B01J8/1836—Heating and cooling the reactor
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07F—ACYCLIC, CARBOCYCLIC OR HETEROCYCLIC COMPOUNDS CONTAINING ELEMENTS OTHER THAN CARBON, HYDROGEN, HALOGEN, OXYGEN, NITROGEN, SULFUR, SELENIUM OR TELLURIUM
- C07F7/00—Compounds containing elements of Groups 4 or 14 of the Periodic Table
- C07F7/02—Silicon compounds
- C07F7/08—Compounds having one or more C—Si linkages
- C07F7/12—Organo silicon halides
- C07F7/16—Preparation thereof from silicon and halogenated hydrocarbons direct synthesis
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The invention belongs to the technical field of reactors, in particular to an organic silicon fluidized bed reactor, which is characterized in that a stirring component and a power component are arranged in the reactor, the stirring component is arranged in the reactor and is used for stirring the materials entering the reactor so as to further ensure the reaction effect of the materials and the gas in the reactor, the power assembly is arranged in the reactor and is positioned below the stirring assembly, and the power assembly is used for providing power for the stirring assembly when the stirring assembly works, the rotation through stirring subassembly stirs the inside material of reactor and reaction gas, improves the reaction efficiency between material and the air current, improves the yield of target product, reduces the possibility of reacting completely and the mixture of incomplete material.
Description
Technical Field
The invention belongs to the technical field of reactors, and particularly relates to an organic silicon fluidized bed reactor.
Background
At present, an organosilicon fluidized bed reactor is generally adopted for the production of industrial organosilicon monomers to carry out catalytic reaction on methyl chloride gas, silicon powder and copper powder, the temperature in the fluidized bed reactor needs to reach 300 ℃ in the reaction process to ensure the reaction, heat is continuously released in the reaction process, solid particles generated by the reaction are discharged from a discharge hole at the bottom of the organosilicon fluidized bed reactor, gas after the reaction is finished is discharged from a gas outlet at the top of the organosilicon fluidized bed reactor, and the produced organosilicon has the performance of both organic materials and inorganic materials and is widely applied to various industries;
the existing organosilicon fluidized bed reactor is provided with a chloromethane air inlet on the side surface of the reactor and a high-temperature gas air inlet on the bottom, silicon powder and copper powder in the reactor are reacted by the chloromethane gas and the high-temperature gas to obtain a silicon compound, because the air inlet directions of the two air inlets are fixed in the working process of the organosilicon fluidized bed, the direction of the gas input into the reactor is single, and because the air flow directions of solid particles and air flow in the continuous flowing process are fixed, the single air flow can cause incomplete reaction of materials and gas in the reactor, the reaction efficiency is not high, and no stirring equipment is arranged in the reactor, the sufficient reaction between the air flow in the reactor and the materials can not be ensured, thereby the reaction efficiency in the equipment is not high, the incompletely reacted materials are easily discharged from a discharge port below the reactor, the yield of the organic silicon is greatly reduced, the reaction is completely mixed with incomplete materials, the subsequent purification of the organic silicon is inconvenient, the production cost is greatly improved, and the waste of resources is caused.
In view of the above, in order to overcome the above technical problems, the present invention designs and develops an organosilicon fluidized bed reactor, which solves the above technical problems.
Disclosure of Invention
The technical problem to be solved by the invention is as follows: the invention provides an organosilicon fluidized bed reactor, which solves the problems that in the working process of an organosilicon fluidized bed, the air inlet directions of two air inlets are fixed, the direction of the gas input into the reactor is single, so that the material distribution in the reactor is uneven, no stirring equipment is arranged in the reactor, and the sufficient reaction between the air flow in the reactor and the material cannot be ensured, so that the efficiency of the internal reaction of equipment is low, the incompletely reacted material is easily discharged from a discharge hole below the reactor, the yield of organosilicon is greatly reduced, the complete reaction and the incomplete material are mixed, the subsequent purification of organosilicon is inconvenient, the production cost is greatly improved, and the resource waste is caused.
The invention provides an organosilicon fluidized bed reactor, which comprises: a reactor, further comprising:
the feed inlet is formed in the left side of the reactor;
the discharge port is formed below the reactor;
the gas outlet is formed above the reactor;
the stirring component is arranged in the reactor and is used for stirring the materials entering the reactor, so that the reaction effect of the materials and gas in the reactor is further ensured;
the power assembly is arranged inside the reactor and below the stirring assembly, and the power assembly is used for providing power for the stirring assembly when the stirring assembly works.
Preferably, the stirring assembly comprises:
the first oil cavity is formed in the upper end inside the reactor, is annular and is fixedly connected with the inner wall of the reactor;
the lower end in the reactor is provided with a second oil cavity, and the second oil cavity is annular and is fixedly connected with the inner wall of the reactor;
the lower end face of the first oil cavity and the upper end face of the second oil cavity are respectively provided with an annular groove;
the sealing gasket is arranged in the annular groove, the cross section of the sealing gasket is I-shaped and is rotationally connected with the annular groove, and the sealing gasket is made of stainless steel;
eight heat oil pipes are arranged between the first oil cavity and the second oil cavity, the upper ends of the eight heat oil pipes are communicated with the first oil cavity through a sealing gasket on the lower end surface of the first oil cavity, the lower ends of the eight heat oil pipes are communicated with the second oil cavity through a sealing gasket on the upper end surface of the second oil cavity, and the eight heat oil pipes are fixedly connected with the sealing gaskets;
the rotating rod is arranged in the reactor and is fixedly connected with the inner end of the connecting rod, and the circle center of the rotating rod is the same as that of the oil cavity;
two layers of connecting rods are arranged between the first oil cavity and the second oil cavity, the inner ends of the connecting rods are fixedly connected with the rotating rod, and the outer ends of the connecting rods are fixedly connected with the hot oil pipe;
the oil outlet is arranged on the left side of the reactor and positioned above the feed inlet, and the inner end of the oil outlet is communicated with the first oil cavity;
the oil inlet is arranged on the left side of the reactor and located below the feed inlet, and the inner end of the oil inlet is communicated with the second oil cavity.
Preferably, the power assembly comprises:
the air cavity comprises a first air cavity and a second air cavity, the air cavity is arranged below the second oil cavity, and the first air cavity, the second air cavity and the inner wall of the reactor are fixedly connected;
the air inlet is arranged on the right side of the reactor, and the inner end of the air inlet is communicated with a second air cavity;
the methyl chloride gas inlet is formed in the left side of the reactor, and the inner end of the methyl chloride gas inlet is communicated with a second air cavity;
the inner walls of the first air cavity and the second air cavity are respectively provided with an air jet, and the air jets are inclined in the clockwise direction on the wall thickness of the air cavities;
the fan, the fan sets up inside the reactor, fan and dwang lower extreme fixed connection.
Preferably, the wall thickness of the corner of the air outlet above the reactor is five centimeters thicker than the side wall of the air outlet.
Preferably, a filter screen is arranged at the air outlet and fixedly connected with the inner wall of the air outlet.
Preferably, an oil outlet of the first oil cavity is fixedly communicated with a heating pipe, and the heating pipe is wound on the outer wall of the feeding hole.
Preferably, the material of the fan is aluminum silicate.
Preferably, the side wall of the air cavity is provided with a plurality of air nozzles.
Preferably, the side wall of the inner end of the air cavity is funnel-shaped, and the lower end of the air cavity is fixedly connected with the discharge hole.
Preferably, the fan blades are flat rectangles.
The invention has the following beneficial effects:
according to the organosilicon fluidized bed reactor provided by the invention, the stirring component and the power component are arranged in the reactor, and the power component below the stirring component provides power for the stirring component, so that the reaction efficiency between materials and airflow in the reactor is ensured, the yield of organosilicon is improved, the possibility of mixing complete reaction and incomplete materials is reduced, and the subsequent processing procedures are guaranteed.
Drawings
The invention will be further explained with reference to the drawings.
FIG. 1 is an overall block diagram of the present invention;
FIG. 2 is a front sectional view of the present invention;
FIG. 3 is a sectional view A-A of the present invention;
FIG. 4 is a sectional view of the invention taken along line B-B;
FIG. 5 is a top view of the fan of the present invention;
FIG. 6 is a representation of the shape of the air outlet of the present invention;
in the figure: the device comprises a reactor 1, a feeding hole 2, a discharging hole 3, an air outlet 4, a first oil cavity 51, a second oil cavity 52, a sealing gasket 6, a hot oil pipe 7, a rotating rod 8, a connecting rod 9, an air cavity 10, a first air cavity 101, a second air cavity 102, a methyl chloride air inlet 11, an air inlet 12, an air jet 13, a fan 14, a filter screen 15, an oil inlet 16, an oil outlet 17, a heating pipe 18 and an annular groove 19.
Detailed Description
To make the objects, technical solutions and advantages of the embodiments of the present invention clearer and more complete description of the technical solutions in the embodiments of the present invention, it is obvious that the described embodiments are some, but not all, embodiments of the present invention. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
The invention provides an organosilicon fluidized bed reactor, which solves the problems that in the working process of a reactor 1, the air inlet directions of two air inlets 2 are fixed, the direction of the gas input into the reactor 1 is single, improper product distribution is caused, the sufficient reaction between the air flow and the materials in the reactor 1 cannot be ensured, and no stirring equipment is arranged in the reactor 1, so that the efficiency of the internal reaction of equipment is low, the materials which are not completely reacted are discharged from a discharge port 3 below the reactor 1 easily, the yield of target products is reduced, the complete reaction and the incomplete reaction are mixed, the subsequent purification of organosilicon is inconvenient, the production cost is greatly increased, and the resource waste is caused.
In order to solve the technical problems, the technical scheme in the embodiment of the invention has the following general idea:
according to the invention, the stirring assembly is arranged in the reactor 1, and the power assembly below the stirring assembly provides power for the stirring assembly, so that the reaction efficiency between materials and air flow in the reactor 1 is ensured, the yield of organic silicon is improved, the possibility of mixing complete reaction and incomplete materials is reduced, and the subsequent processing procedures are guaranteed.
In order to make the technical means, the creation characteristics, the achievement purposes and the effects of the invention easy to understand, the invention is further described with the specific embodiments.
The present invention provides an organosilicon fluidized bed reactor comprising: the reactor 1, further comprising:
the feed inlet 2 is formed in the left side of the reactor 1;
the discharge port 3 is formed below the reactor 1;
the gas outlet 4 is formed above the reactor 1;
the stirring component is arranged in the reactor 1 and is used for stirring the materials entering the reactor 1 so as to further ensure the reaction effect of the materials and the gas in the reactor 1;
the power assembly is arranged in the reactor 1 and is positioned below the stirring assembly, and the power assembly is used for providing power for the stirring assembly when the stirring assembly works.
According to the invention, the stirring assembly and the power assembly for providing power for the stirring assembly are arranged in the reactor 1, and the materials and the reaction gas in the reactor 1 are stirred by the rotation of the stirring assembly, so that the reaction efficiency between the materials and the gas flow is improved, the yield of the target product is improved, and the possibility of mixing the complete reaction and the incomplete reaction materials is reduced.
As a specific embodiment of the present invention, the stirring assembly includes:
the first oil chamber 51 is formed in the upper end inside the reactor 1, and the first oil chamber 51 is annular and is fixedly connected with the inner wall of the reactor 1;
the second oil cavity 52 is formed in the lower end inside the reactor 1, and the second oil cavity 52 is annular and is fixedly connected with the inner wall of the reactor 1;
the annular groove 19 is formed in the lower end surface of the first oil cavity 51 and the upper end surface of the second oil cavity 52 respectively;
the sealing gasket 6 is arranged in the annular groove 19, the cross section of the sealing gasket 6 is I-shaped and is rotationally connected with the annular groove 19, and the sealing gasket 6 is made of stainless steel;
eight heat oil pipes 7 are arranged between the first oil cavity 51 and the second oil cavity 52, the upper ends of the eight heat oil pipes 7 penetrate through a sealing gasket 6 on the lower end face of the first oil cavity 51 to be communicated with the first oil cavity 51, the lower ends of the eight heat oil pipes 7 penetrate through a sealing gasket 6 on the upper end face of the second oil cavity 52 to be communicated with the second oil cavity 52, and the eight heat oil pipes 7 are fixedly connected with the sealing gasket 6;
the rotating rod 8 is arranged in the reactor 1 and is fixedly connected with the inner end of the connecting rod 9, and the circle center of the rotating rod 8 is the same as that of the oil cavity 5;
two layers of connecting rods 9 are arranged between the first oil cavity 51 and the second oil cavity 52, the inner ends of the connecting rods 9 are fixedly connected with the rotating rod 8, and the outer ends of the connecting rods 9 are fixedly connected with the hot oil pipe 7;
the oil outlet 17 is arranged at the left side of the reactor 1 and is positioned above the feed inlet 2, and the inner end of the oil outlet 17 is communicated with a first oil cavity 51;
the oil inlet 16 is arranged on the left side of the reactor 1 and is positioned below the feed inlet 2, and the inner end of the oil inlet 16 is communicated with the second oil cavity 52.
In the working process of the invention, through the rotation of the rotating rod 8, the rotating rod 8 is arranged in the reactor 1 and is fixedly connected with the inner end of the connecting rod 9, the circle center of the rotating rod 8 is the same as the circle center of the oil chamber 5, the rotation of the rotating rod 8 drives the connecting rod 9 to rotate, two layers of connecting rods 9 are arranged between the first oil chamber 51 and the second oil chamber 52, the inner end of the connecting rod 9 is fixedly connected with the rotating rod 8, the outer end of the connecting rod 9 is fixedly connected with the hot oil pipe 7, the rotation of the hot oil pipe 7 is driven through the rotation of the connecting rod 9, eight hot oil pipes 7 are arranged between the first oil chamber 51 and the second oil chamber 52, the upper ends of the eight hot oil pipes 7 pass through the sealing gasket 6 on the lower end face of the first oil chamber 51 and are mutually communicated with the first oil chamber 51, the lower ends of the eight hot oil pipes 7 pass through the sealing gasket 6 on the upper end face of the second oil chamber 52 and are mutually communicated with the second oil chamber 52, and the eight hot oil pipes 7 are fixedly connected with the sealing gasket 6, the rotation of the sealing gasket 6 is driven by the rotation of the hot oil pipes 7, the annular groove 19 is respectively arranged on the lower end surface of the first oil cavity 51 and the upper end surface of the second oil cavity 52, the annular sealing gasket 6 is arranged in the annular groove 19, the cross section of the sealing gasket 6 is in an I shape and is rotatably connected with the annular groove 19, the rotating rod 8 drives the hot oil pipes 7 to rotate by the connecting rod 9, the rotation of the hot oil pipes 7 drives the sealing gasket 6 to rotate, the sealing gasket 6 is rotatably connected with the annular groove 19, so that the hot oil pipes 7 can rotate relative to the first oil cavity 51 and the second oil cavity 52, the first oil cavity 51 is arranged at the upper end in the reactor 1, the first oil cavity 51 is annular and is fixedly connected with the inner wall of the reactor 1, and the second oil cavity 52 is arranged at the lower end in the reactor 1, the second oil cavity 52 is annular and is fixedly connected with the inner wall of the reactor 1, materials and airflow in the reactor 1 are stirred through the rotation of the hot oil pipe 7, the reaction speed between the airflow and the materials is further improved through stirring, the reaction efficiency between the materials and the airflow is further improved, and the yield of target products is ensured. When the oil in the first oil cavity 51 reaches the same horizontal position as the oil outlet 17 communicated with the first oil cavity 51, the heat conducting oil in the first oil cavity 51 flows out of the first oil cavity 51 through the oil outlet 17, the flowing heat conducting oil is conveyed into the cooling pool for cooling, and the cooled oil is conveyed into the second oil cavity 52 through the oil pump, so that the circulation of the heat conducting oil is completed, the temperature of the input heat conducting oil is far lower than that of the heat conducting oil in the first oil cavity 51 and the second oil cavity 52, the temperature of the heat conducting oil in the first oil cavity 51 and the second oil cavity 52 is reduced through the input heat conducting oil, so that the possibility that the reaction is too violent and the danger is caused due to the overhigh temperature of the heat conducting oil in the first oil cavity 51 and the second oil cavity 52 is avoided, when materials enter the reactor 1 to react with the high-temperature gas and the methyl chloride gas in the reactor 1, the heat emitted by the heat oil pipe 7, the heat conducting oil in the hot oil pipe 7 continuously absorbs heat in the process of moving upwards, the heat conducting oil is conveyed to the first oil cavity 51 and then discharged to the outside of the reactor 1 through the oil outlet 17 for cooling, the cooled heat conducting oil is conveyed to the second oil cavity 52 through the oil inlet 16, the heat conducting oil in the second oil cavity 52 is conveyed to the first oil cavity 51 through the hot oil pipe 7, the circulation is repeated, the absorption of redundant heat in the reaction process is completed, byproducts generated in the reaction are prevented from being heated, decomposed and carbonized in a high-temperature state, and granular silicon powder is carbonized into blocks, so that the reaction is influenced, the sealing gasket is made of stainless steel, the sealing gasket can work in a 700 ℃ state, the sealing gasket 6 is prevented from being damaged by high temperature in the working process, the first oil cavity 51 and the second oil cavity 52 are annular, the gas after the reaction is moved upwards from the region in the middle of the annular first oil cavity 51 and then discharged from the gas outlet 4, the reacted materials fall downwards from the middle area of the second oil cavity 52 ring and are discharged from the discharge port 3, and the materials enter the reactor 1 from the feed port 2 in the working process and then react with methyl chloride gas and high-temperature gas in the reactor 1, because the air flow in the reactor 1 is spiral, compared with the existing organosilicon fluidized bed reactor 1, the direct impact of the air flow in the reactor 1 on the materials is avoided, the materials can be ensured to fall downwards under the action of gravity, so that the reactants generated after the reaction are discharged from the discharge port 3, the reaction work is completed, the flow direction of the heat conducting oil in the heat oil pipe 7 is fixed, the condition that the heat exchange between the surface of the heat oil pipe 7 and the heat conducting oil is not uniform is avoided, and the condition that the reaction is intensified due to local overheating caused by the nonuniform temperature in the reactor 1 is avoided, the normal operation of the reaction is ensured, the structure of the sealing gasket 6 is I-shaped, the sealing gasket 6 is positioned by the matching of the sealing gasket 6 and the annular groove 19, so that the situation that the sealing gasket 6 on the lower end surface of the first oil cavity 51 falls downwards relative to the first oil cavity 51 due to the gravity of the hot oil pipe 7 is ensured, the second oil cavity 52 supports the sealing gasket 6 on the upper end surface of the second oil cavity 52, the sealing gasket 6 is ensured not to fluctuate up and down in the working process, the normal operation of the hot oil pipe 7 is ensured, and the oil in the oil cavity 5 is ensured not to leak into the reactor 1 through the action of the sealing gasket 6, so that the reaction is influenced, the rotatable hot oil pipe 7 is arranged in the reactor 1, and on the premise of ensuring the cooling function of the hot oil pipe 7, the hot oil pipe 7 is driven to rotate by air flow, the materials and the gas flow in the reactor 1 are stirred, so that the reaction speed between the materials and the gas flow is further improved, the reaction efficiency is ensured, the possibility of incomplete reaction is reduced, and the yield of the target product is further ensured.
As a specific embodiment of the present invention, the power module includes:
the air cavity 10 comprises a first air cavity 101 and a second air cavity 102, the air cavity 10 is arranged below the second oil cavity 52, and the first air cavity 101 and the second air cavity 102 are fixedly connected with the inner wall of the reactor 1;
the air inlet 12 is arranged on the right side of the reactor 1, and the inner end of the air inlet 12 is communicated with a second air cavity 101;
the methyl chloride gas inlet 11 is arranged on the left side of the reactor 1, and the inner end of the methyl chloride gas inlet 11 is communicated with a second air cavity 102;
the inner walls of the first air cavity 101 and the second air cavity 102 are respectively provided with an air jet 13, and the air jet 13 is inclined in the clockwise direction on the wall thickness of the air cavity 10;
and the fan 14 is arranged in the reactor 1, and the fan 14 is fixedly connected with the lower end of the rotating rod 8.
In the working process of the invention, a first air cavity 101 and a second air cavity 102 are arranged below the second oil cavity 52, the first air cavity 101, the second air cavity 102 and the inner wall of the reactor 1 are fixedly connected, the fan 14 is arranged in the reactor 1, the fan 14 is fixedly connected with the lower end of the rotating rod 8, when the work is started, the methyl chloride air inlet 11 is arranged at the left side of the reactor 1, the inner end of the methyl chloride air inlet 11 is communicated with the second air cavity 102, methyl chloride gas enters the first air cavity 101 through the methyl chloride air inlet 11, the air inlet 12 is arranged at the right side of the reactor 1, the inner end of the air inlet 12 is communicated with the second air cavity 102, high-temperature gas conveys the gas flow to the second air cavity 102 through the air inlet 12, and along with the continuous input of the methyl chloride gas and the high-temperature gas, the gas in the first air cavity 101 and the second air cavity 102 enters the reactor 1 through the gas jet ports 13 at the inner wall of the air cavities 10 under the action of the air pressure of the air cavities, the inner walls of the first air cavity 101 and the second air cavity 102 are respectively provided with an air jet 13, the air jet 13 is inclined along the clockwise direction on the wall thickness of the air cavity 10, when the air in the air cavity 10 passes through the air jet 13, the air flow of the right side air jet 13 is blown to the upper left, and the air flow of the left side air jet 13 is blown to the upper right, so that the air flow sprayed from the air cavity 10 forms a rotating air flow which is observed to be anticlockwise from the top, the rotating air flow drives the material entering from the feed port 2 to rotate in the ascending process, the material reacts under the action of high-temperature gas and methyl chloride gas, the flowing of the rotating air flow drives the rotation of the fan 14, the fan 14 is arranged in the reactor 1, the fan 14 is fixedly connected with the lower end of the rotating rod 8, the rotation of the fan 14 is driven by the air flow, and the rotating rod 8 fixedly connected with the fan 14 is driven to rotate, rotation through dwang 8 drives the rotation of heat oil pipe 7, the rotation through heat oil pipe 7 stirs 1 inside material and air current of reactor, contact between material and the air current has further been guaranteed through 1 inside rotatory air current of reactor, and the rotation that drives heat oil pipe 7 through the air current stirs 1 inside material of reactor, reaction rate has further been accelerated, thereby the effect of reaction has been guaranteed when having improved the efficiency of reaction, the possibility of incomplete reaction has been reduced, the yield of target product has further been guaranteed.
As a specific embodiment of the invention, the wall thickness of the corner of the gas outlet 4 above the reactor 1 is five centimeters thicker than that of the side wall of the gas outlet 4.
In the working process of the invention, part of materials are inevitably carried along with the rising of the airflow in the reactor 1 and are discharged from the air outlet 4, the main components of the materials are silicon powder, copper powder or silicon compounds, wherein the hardness of the silicon powder is higher, the airflow carrying the silicon powder collides at the bent part of the pipeline, so that the abrasion of the bent part of the pipeline is further intensified, and the leakage condition occurs, the wall thickness of the bent part of the air outlet 4 above the reactor 1 is five centimeters thicker than the side wall of the air outlet 4, the safety of the equipment is further ensured, the leakage possibility of the equipment is reduced, and the long-term use of the equipment is ensured.
As a specific embodiment of the present invention, a filter screen 15 is disposed at the air outlet 4, and the filter screen 15 is fixedly connected to the inner wall of the air outlet 4.
In the working process of the invention, the air flow after the reaction is finished is discharged from the air outlet 4 above the reactor 1, part of materials are inevitably carried in the discharged air flow, the filter screen 15 is arranged at the air outlet 4, the filter screen 15 is fixedly connected with the inner wall of the air outlet 4, on one hand, the condition that the materials are discharged out of the reactor 1 is greatly reduced through the filter screen 15, most of the materials are intercepted, the possibility of resource waste is reduced, on the other hand, the diameter of the discharged materials is reduced, and the abrasion of the discharged materials to the bent part of the pipeline is reduced, thereby ensuring the safety and long-term use of the equipment.
As a specific embodiment of the present invention, the oil outlet 17 of the first oil chamber 51 is fixedly communicated with a heating pipe 18, and the heating pipe 18 is wound on the outer wall of the feed port 2.
In the working process, the temperature inside the reactor 1 is absorbed through the hot oil pipe 7, the heat conducting oil inside the hot oil pipe 7 is conveyed into the first oil cavity 51, and the heat conducting oil is discharged through the oil outlet 17, because the temperature of the heat conducting oil in the first oil cavity 51 is higher than the normal temperature, the material at the feeding hole 2 is preheated by utilizing the waste heat of the heat conducting oil through winding the heating pipe 18 fixedly communicated with the oil outlet 17 of the first oil cavity 51 on the outer wall of the feeding hole 2, the temperature of the material when the material enters the reactor 1 is ensured, the reaction speed of the material with potassium chloride gas and high-temperature gas is improved, and the reaction speed and the effect of the reactor 1 are further improved.
In one embodiment of the present invention, the material of the fan 14 is aluminum silicate.
In the working process of the invention, the temperature in the reactor 1 is high, heat is continuously released in the reaction process, the fan 14 is made of aluminum silicate, on one hand, the aluminum silicate has low density, so that the weight of the fan 14 is reduced, the load of the rotating rod 8 fixedly connected with the fan 14 is greatly reduced, and the possibility that the rotating rod 8 falls down due to the overweight of the fan 14 is avoided, on the other hand, the aluminum silicate is high-temperature resistant, so that the fan 14 can be prevented from being damaged by the high temperature released in the reaction process, and meanwhile, the aluminum silicate is not easy to react with the materials and the airflow in the reactor 1, so that the purity of the product is ensured.
In one embodiment of the present invention, the side wall of the air chamber 10 is provided with a plurality of air injection ports 13.
In the working process of the invention, the fan 14 in the reactor 1 is driven to rotate by the airflow ejected from the air ejection openings 13 on the side wall of the air cavity 10, the side wall of the air cavity 10 is provided with a plurality of air ejection openings 13, and when the first air cavity 101 and the second air cavity 102 work, the airflow is respectively ejected from the first air cavity 101 and the second air cavity 102 simultaneously, the two air cavities 10 simultaneously blow air to increase the flowing speed of the air and reduce the possibility of single airflow direction caused by a single air cavity 10, on the other hand, the side wall of the air cavity 10 is provided with a plurality of air ejection openings 13, so that the airflow ejected from the air cavity 10 is more uniform and more efficient, the condition that the airflow direction ejected from the single air ejection opening 13 is single and the efficiency is low is avoided, the reaction efficiency is further improved by ejecting air through the plurality of air ejection openings 13, and the ejected airflow is more uniform and stable to ensure that the rotating speed of the fan 14 is more uniform, the possibility that the fan 14 is blown by the airflow and damaged due to the large airflow impact force and the large airflow speed change of the airflow ejected by the single air nozzle 13 is avoided.
As a specific embodiment of the present invention, the inner end sidewall of the air cavity 10 is funnel-shaped, and the lower end is fixedly connected to the discharge hole 3.
In the working process of the invention, the gas in the air cavity 10 reacts with the materials, the reacted materials fall downwards from the region in the middle of the ring of the second oil cavity 52 and are discharged from the discharge port 3, part of the materials fall on the inner wall of the air cavity 10, the inner end side wall of the air cavity 10 is funnel-shaped, the lower end of the air cavity is fixedly connected with the discharge port 3, the materials falling on the inner wall of the air cavity 10 slide downwards under the action of gravity and are discharged from the discharge port 3, and the pneumatic force sprayed by the gas nozzle 13 is smaller than the gravity of the reacted materials, so that on one hand, the materials can be discharged from the discharge port 3 under the action of gravity and cannot fall into the air cavity 10, on the other hand, the gas flow rate is not too high, the materials are prevented from being blown into the gas nozzle 4 by the gas flow, and the normal reaction of the materials is ensured.
In an embodiment of the present invention, the fan 14 has a flat rectangular shape.
In the working process of the invention, the fan 14 is driven to rotate by the airflow in the reactor 1, so as to drive the rotating rod 8 to rotate, the fan blades of the fan 14 are flat rectangles, on one hand, the rectangular fan blades have large stress area, which is more beneficial to the rotation of the fan 14 driven by the airflow sprayed by the air cavity 10, on the other hand, the material can fall on the fan blades in the falling process, the quantity of the material accumulated on the flat rectangular fan blades is greatly reduced, and along with the rotation of the fan 14 and the blowing of the airflow, the possibility of the material accumulated on the fan blades of the fan 14 is further reduced, and most of the material can be normally discharged from the discharge hole 3.
The working principle is as follows: according to the invention, the stirring assembly and the power assembly for providing power for the stirring assembly are arranged in the reactor 1, and the materials and the reaction gas in the reactor 1 are stirred by the rotation of the stirring assembly, so that the reaction efficiency between the materials and the gas flow is improved, the yield of a target product is improved, and the possibility of mixing the complete reaction and the incomplete reaction materials is reduced;
in the working process of the invention, through the rotation of the rotating rod 8, the rotating rod 8 is arranged in the reactor 1 and is fixedly connected with the inner end of the connecting rod 9, the circle center of the rotating rod 8 is the same as the circle center of the oil chamber 5, the rotation of the rotating rod 8 drives the connecting rod 9 to rotate, two layers of connecting rods 9 are arranged between the first oil chamber 51 and the second oil chamber 52, the inner end of the connecting rod 9 is fixedly connected with the rotating rod 8, the outer end of the connecting rod 9 is fixedly connected with the hot oil pipe 7, the rotation of the hot oil pipe 7 is driven through the rotation of the connecting rod 9, eight hot oil pipes 7 are arranged between the first oil chamber 51 and the second oil chamber 52, the upper ends of the eight hot oil pipes 7 pass through the sealing gasket 6 on the lower end face of the first oil chamber 51 and are mutually communicated with the first oil chamber 51, the lower ends of the eight hot oil pipes 7 pass through the sealing gasket 6 on the upper end face of the second oil chamber 52 and are mutually communicated with the second oil chamber 52, and the eight hot oil pipes 7 are fixedly connected with the sealing gasket 6, the rotation of the sealing gasket 6 is driven by the rotation of the hot oil pipes 7, the annular groove 19 is respectively arranged on the lower end surface of the first oil cavity 51 and the upper end surface of the second oil cavity 52, the annular sealing gasket 6 is arranged in the annular groove 19, the cross section of the sealing gasket 6 is in an I shape and is rotatably connected with the annular groove 19, the rotating rod 8 drives the hot oil pipes 7 to rotate by the connecting rod 9, the rotation of the hot oil pipes 7 drives the sealing gasket 6 to rotate, the sealing gasket 6 is rotatably connected with the annular groove 19, so that the hot oil pipes 7 can rotate relative to the first oil cavity 51 and the second oil cavity 52, the first oil cavity 51 is arranged at the upper end in the reactor 1, the first oil cavity 51 is annular and is fixedly connected with the inner wall of the reactor 1, and the second oil cavity 52 is arranged at the lower end in the reactor 1, the second oil cavity 52 is annular and is fixedly connected with the inner wall of the reactor 1, materials and airflow in the reactor 1 are stirred through the rotation of the hot oil pipe 7, the reaction speed between the airflow and the materials is further improved through stirring, the reaction efficiency between the materials and the airflow is further improved, and the yield of target products is ensured, the cooled heat conduction oil is conveyed into the second oil cavity 52 through the oil inlet 16 through the oil pump, when the heat conduction oil in the second oil cavity 52 is full, the heat conduction oil is continuously input to increase the oil pressure in the second oil cavity 52, the continuously input oil enters the hot oil pipe 7 through the lower port of the hot oil pipe 7 communicated with the second oil cavity 52 under the action of pressure, and along with the input of the heat conduction oil, the heat conduction oil in the hot oil pipe 7 enters the first oil cavity 51 through the upper port of the hot oil pipe 7 communicated with the first oil cavity 51, when the oil in the first oil cavity 51 reaches the same horizontal position as the oil outlet 17 communicated with the first oil cavity 51, the heat conducting oil in the first oil cavity 51 flows out of the first oil cavity 51 through the oil outlet 17, the flowing heat conducting oil is conveyed into the cooling pool for cooling, and the cooled oil is conveyed into the second oil cavity 52 through the oil pump, so that the circulation of the heat conducting oil is completed, the temperature of the input heat conducting oil is far lower than that of the heat conducting oil in the first oil cavity 51 and the second oil cavity 52, the temperature of the heat conducting oil in the first oil cavity 51 and the second oil cavity 52 is reduced through the input heat conducting oil, so that the possibility that the reaction is too violent and the danger is caused due to the overhigh temperature of the heat conducting oil in the first oil cavity 51 and the second oil cavity 52 is avoided, when materials enter the reactor 1 to react with the high-temperature gas and the methyl chloride gas in the reactor 1, the heat emitted by the heat oil pipe 7, the heat conducting oil in the hot oil pipe 7 continuously absorbs heat in the process of moving upwards, the heat conducting oil is conveyed to the first oil cavity 51 and then discharged to the outside of the reactor 1 through the oil outlet 17 for cooling, the cooled heat conducting oil is conveyed to the second oil cavity 52 through the oil inlet 16, the heat conducting oil in the second oil cavity 52 is conveyed to the first oil cavity 51 through the hot oil pipe 7, the circulation is repeated, the absorption of redundant heat in the reaction process is completed, byproducts generated in the reaction are prevented from being heated, decomposed and carbonized in a high-temperature state, and granular silicon powder is carbonized into blocks, so that the reaction is influenced, the sealing gasket is made of stainless steel, the sealing gasket can work in a 700 ℃ state, the sealing gasket 6 is prevented from being damaged by high temperature in the working process, the first oil cavity 51 and the second oil cavity 52 are annular, the gas after the reaction is moved upwards from the region in the middle of the annular first oil cavity 51 and then discharged from the gas outlet 4, the reacted materials fall downwards from the middle area of the second oil cavity 52 ring and are discharged from the discharge port 3, and the materials enter the reactor 1 from the feed port 2 in the working process and then react with methyl chloride gas and high-temperature gas in the reactor 1, because the air flow in the reactor 1 is spiral, compared with the existing organosilicon fluidized bed reactor 1, the direct impact of the air flow in the reactor 1 on the materials is avoided, the materials can be ensured to fall downwards under the action of gravity, so that the reactants generated after the reaction are discharged from the discharge port 3, the reaction work is completed, the flow direction of the heat conducting oil in the heat oil pipe 7 is fixed, the condition that the heat exchange between the surface of the heat oil pipe 7 and the heat conducting oil is not uniform is avoided, and the condition that the reaction is intensified due to local overheating caused by the nonuniform temperature in the reactor 1 is avoided, the normal operation of the reaction is ensured, the structure of the sealing gasket 6 is I-shaped, the sealing gasket 6 is positioned by the matching of the sealing gasket 6 and the annular groove 19, so that the situation that the sealing gasket 6 on the lower end surface of the first oil cavity 51 falls downwards relative to the first oil cavity 51 due to the gravity of the hot oil pipe 7 is ensured, the second oil cavity 52 supports the sealing gasket 6 on the upper end surface of the second oil cavity 52, the sealing gasket 6 is ensured not to fluctuate up and down in the working process, the normal operation of the hot oil pipe 7 is ensured, and the oil in the oil cavity 5 is ensured not to leak into the reactor 1 through the action of the sealing gasket 6, so that the reaction is influenced, the rotatable hot oil pipe 7 is arranged in the reactor 1, and on the premise of ensuring the cooling function of the hot oil pipe 7, the hot oil pipe 7 is driven to rotate by air flow, the materials and the gas flow in the reactor 1 are stirred, so that the reaction speed between the materials and the gas flow is further improved, the reaction efficiency is ensured, the possibility of incomplete reaction is reduced, and the yield of the target product is further ensured;
and in the working process, a first air cavity 101 and a second air cavity 102 are arranged below the second oil cavity 52, the first air cavity 101, the second air cavity 102 and the inner wall of the reactor 1 are fixedly connected, the fan 14 is arranged in the reactor 1, the fan 14 is fixedly connected with the lower end of the rotating rod 8, when the working starts, the methyl chloride air inlet 11 is arranged on the left side of the reactor 1, the inner end of the methyl chloride air inlet 11 is communicated with the second air cavity 102, methyl chloride gas enters the first air cavity 101 through the methyl chloride air inlet 11, the air inlet 12 is arranged on the right side of the reactor 1, the inner end of the air inlet 12 is communicated with the second air cavity 102, high-temperature gas conveys the gas flow to the second air cavity 102 through the air inlet 12, and along with the continuous input of the methyl chloride gas and the high-temperature gas, the gas in the first air cavity 101 and the second air cavity 102 enters the reactor 1 through the gas jet ports 13 on the inner wall of the air cavities 10 under the action of the air pressure, the inner walls of the first air cavity 101 and the second air cavity 102 are respectively provided with an air jet 13, the air jet 13 is inclined along the clockwise direction on the wall thickness of the air cavity 10, when the air in the air cavity 10 passes through the air jet 13, the air flow of the right side air jet 13 is blown to the upper left, and the air flow of the left side air jet 13 is blown to the upper right, so that the air flow sprayed from the air cavity 10 forms a rotating air flow which is observed to be anticlockwise from the top, the rotating air flow drives the material entering from the feed port 2 to rotate in the ascending process, the material reacts under the action of high-temperature gas and methyl chloride gas, the flowing of the rotating air flow drives the rotation of the fan 14, the fan 14 is arranged in the reactor 1, the fan 14 is fixedly connected with the lower end of the rotating rod 8, the rotation of the fan 14 is driven by the air flow, and the rotating rod 8 fixedly connected with the fan 14 is driven to rotate, the rotation of the rotating rod 8 drives the rotation of the hot oil pipe 7, the materials and the air flow in the reactor 1 are stirred through the rotation of the hot oil pipe 7, the contact between the materials and the air flow is further ensured through the rotating air flow in the reactor 1, and the materials in the reactor 1 are stirred through the rotation of the hot oil pipe 7 driven by the air flow, so that the reaction rate is further accelerated, the reaction effect is ensured while the reaction efficiency is improved, the possibility of incomplete reaction is reduced, and the yield of target products is further ensured;
for long-term use of the equipment, the gas flow in the reactor 1 inevitably carries part of materials to be discharged from the gas outlet 4 along with rising of the gas flow, the main components of the materials are silicon powder, copper powder or silicon compounds, wherein the silicon powder has higher hardness, the gas flow carrying the silicon powder collides at the bent part of the pipeline to further aggravate the abrasion of the bent part of the pipeline, so that leakage occurs, the wall thickness of the bent part of the gas outlet 4 above the reactor 1 is five centimeters thicker than the side wall of the gas outlet 4, the safety of the equipment is further ensured, the possibility of equipment leakage is reduced, and the long-term use of the equipment is ensured;
in the working process, the air flow after the reaction is finished is discharged from the air outlet 4 above the reactor 1, part of materials are inevitably carried in the discharged air flow, the filter screen 15 is arranged at the air outlet 4, the filter screen 15 is fixedly connected with the inner wall of the air outlet 4, on one hand, the condition that the materials are discharged out of the reactor 1 is greatly reduced through the filter screen 15, most of the materials are intercepted, the possibility of resource waste is reduced, on the other hand, the diameter of the discharged materials is reduced, and the abrasion of the discharged materials to the bent part of a pipeline is reduced, so that the safety and the long-term use of equipment are ensured;
in order to further ensure the reaction effect, the temperature inside the reactor 1 is absorbed through the hot oil pipe 7, then the heat conducting oil inside the hot oil pipe 7 is conveyed into the first oil cavity 51, and then the heat conducting oil is discharged through the oil outlet 17, because the temperature of the heat conducting oil in the first oil cavity 51 is higher than the normal temperature, the heating pipe 18 fixedly communicated with the oil outlet 17 of the first oil cavity 51 is wound on the outer wall of the feeding hole 2, the material at the feeding hole 2 is preheated by utilizing the waste heat of the heat conducting oil, the temperature of the material when entering the reactor 1 is ensured, the reaction speed of the material with potassium chloride gas and high-temperature gas is improved, and the reaction speed and the effect of the reactor 1 are further improved;
in the working process, the temperature in the reactor 1 is high, heat is continuously released in the reaction process, the fan 14 is made of aluminum silicate, the aluminum silicate has low density, the weight of the fan 14 is reduced, the load of a rotating rod 8 fixedly connected with the fan 14 is greatly reduced, the possibility that the rotating rod 8 falls off due to the fact that the fan 14 is too heavy is avoided, and the aluminum silicate is high-temperature resistant, so that the fan 14 can be prevented from being damaged by the high temperature released in the reaction process, and meanwhile, the aluminum silicate is not easy to react with materials and airflow in the reactor 1, so that the purity of a product is ensured;
in the working process of the invention, the fan 14 in the reactor 1 is driven to rotate by the airflow ejected from the air nozzles 13 on the side wall of the air cavity 10, the side wall of the air cavity 10 is provided with a plurality of air nozzles 13, and when the first air cavity 101 and the second air cavity 102 work, the airflow is respectively blown out from the first air cavity 101 and the second air cavity 102 simultaneously, the two air cavities 10 blow simultaneously to increase the flowing speed of the air and reduce the possibility of single airflow direction caused by a single air cavity 10, on the other hand, the side wall of the air cavity 10 is provided with a plurality of air nozzles 13, so that the airflow ejected from the air cavity 10 is more uniform and higher in efficiency, the conditions of single airflow direction and low efficiency of the airflow ejected from a single air nozzle 13 are avoided, the reaction efficiency is further improved by ejecting air through a plurality of air nozzles 13, and the rotating speed of the fan 14 is more uniform and stable by ejecting the airflow at the same time, the possibility that the fan 14 is blown by airflow and damaged due to large airflow impact force sprayed by a single air nozzle 13 and large airflow speed change is avoided;
in the working process, the gas inside the air cavity 10 reacts with the materials, the reacted materials fall downwards from the region in the middle of the ring of the second oil cavity 52 and are discharged from the discharge port 3, part of the materials fall on the inner wall of the air cavity 10, the inner end side wall of the air cavity 10 is funnel-shaped, the lower end of the air cavity is fixedly connected with the discharge port 3, the materials falling on the inner wall of the air cavity 10 slide downwards under the action of gravity and are discharged from the discharge port 3, and the pneumatic force sprayed by the gas nozzle 13 is smaller than the gravity of the reacted materials, so that the materials can be discharged from the discharge port 3 under the action of gravity and cannot fall inside the air cavity 10, the gas flow rate is not too high, the materials are prevented from being blown into the gas outlet 4 by the gas flow, and the normal reaction of the materials is ensured;
in the working process of the invention, the fan 14 is driven to rotate by the airflow in the reactor 1, so as to drive the rotating rod 8 to rotate, the fan blades of the fan 14 are flat rectangles, on one hand, the rectangular fan blades have large stress area, which is more beneficial to the rotation of the fan 14 driven by the airflow sprayed by the air cavity 10, on the other hand, the material can fall on the fan blades in the falling process, the quantity of the material accumulated on the flat rectangular fan blades is greatly reduced, and along with the rotation of the fan 14 and the blowing of the airflow, the possibility of the material accumulated on the fan blades of the fan 14 is further reduced, and most of the material can be normally discharged from the discharge hole 3.
The foregoing illustrates and describes the principles, general features, and advantages of the present invention. It will be understood by those skilled in the art that the present invention is not limited to the embodiments described above, which are described in the specification and illustrated only to illustrate the principle of the present invention, but that various changes and modifications may be made therein without departing from the spirit and scope of the present invention, which fall within the scope of the invention as claimed. The scope of the invention is defined by the appended claims and equivalents thereof.
Claims (10)
1. An organosilicon fluidized bed reactor, comprising a reactor (1), characterized by further comprising:
the feeding hole (2), the feeding hole (2) is arranged at the left side of the reactor (1);
the discharge port (3), the discharge port (3) is arranged below the reactor (1);
the gas outlet (4), the gas outlet (4) is arranged above the reactor (1);
the stirring component is arranged in the reactor and is used for stirring the materials entering the reactor, so that the reaction effect of the materials and gas in the reactor is further ensured;
the power assembly is arranged in the reactor and is positioned below the stirring assembly, and the power assembly is used for providing power for the stirring assembly when the stirring assembly works.
2. A silicone fluidized bed reactor as set forth in claim 1, wherein: the stirring subassembly includes:
the first oil cavity (51) is formed in the upper end inside the reactor (1), and the first oil cavity (51) is annular and is fixedly connected with the inner wall of the reactor (1);
the second oil cavity (52) is formed in the lower end of the interior of the reactor (1), and the second oil cavity (52) is annular and is fixedly connected with the inner wall of the reactor (1);
the annular groove (19) is formed in the lower end face of the first oil cavity (51) and the upper end face of the second oil cavity (52) respectively;
the sealing device comprises a sealing gasket (6), wherein an annular sealing gasket (6) is arranged in the annular groove (19), the cross section of the sealing gasket (6) is I-shaped and is rotationally connected with the annular groove (19), and the sealing gasket (6) is made of stainless steel;
eight heat oil pipes (7) are arranged between the first oil cavity (51) and the second oil cavity (52), the upper ends of the eight heat oil pipes (7) penetrate through a sealing gasket (6) on the lower end face of the first oil cavity (51) to be communicated with the first oil cavity (51), the lower ends of the eight heat oil pipes (7) penetrate through a sealing gasket (6) on the upper end face of the second oil cavity (52) to be communicated with the second oil cavity (52), and the eight heat oil pipes (7) are fixedly connected with the sealing gasket (6);
the rotating rod (8) is arranged in the reactor (1) and is fixedly connected with the inner end of the annular connecting rod (9), and the circle center of the rotating rod (8) is the same as that of the oil cavity (5);
two layers of annular connecting rods (9) are arranged between the first oil cavity (51) and the second oil cavity (52), the inner ends of the annular connecting rods (9) are fixedly connected with the rotating rod (8), and the outer ends of the annular connecting rods (9) are fixedly connected with the hot oil pipe (7);
the oil outlet (17) is arranged on the left side of the reactor (1) and is positioned above the feed port (2), and the inner end of the oil outlet (17) is communicated with an oil cavity I (51);
the oil inlet (16) is arranged on the left side of the reactor (1) and is located below the feed inlet (2), and the inner end of the oil inlet (16) is communicated with the second oil cavity (52).
3. A silicone fluidized bed reactor as set forth in claim 2, wherein: the power assembly includes:
the air cavity (10) comprises a first air cavity (101) and a second air cavity (102), the air cavity (10) is arranged below the second oil cavity (52), and the first air cavity (101) and the second air cavity (102) are fixedly connected with the inner wall of the reactor (1);
the gas inlet (12), the gas inlet (12) is arranged on the right side of the reactor (1), and the inner end of the gas inlet (12) is communicated with a second gas cavity (101);
the methane chloride gas inlet (11), the methane chloride gas inlet (11) is arranged on the left side of the reactor (1), and the inner end of the methane chloride gas inlet (11) is communicated with the second air cavity (102);
the inner walls of the first air cavity (101) and the second air cavity (102) are respectively provided with an air jet (13), and the air jet (13) is inclined in the clockwise direction on the wall thickness of the air cavity (10);
the fan (14), fan (14) set up inside reactor (1), fan (14) and dwang (8) lower extreme fixed connection.
4. A silicone fluidized bed reactor as set forth in claim 1, wherein: the wall thickness of the turning part of the air outlet (4) above the reactor (1) is five centimeters thicker than the side wall of the air outlet (4).
5. A silicone fluidized bed reactor as set forth in claim 1, wherein: and a filter screen (15) is arranged at the air outlet (4), and the filter screen (15) is fixedly connected with the inner wall of the air outlet (4).
6. A silicone fluidized bed reactor as set forth in claim 2, characterized in that: an oil outlet (17) of the first oil chamber (51) is fixedly communicated with a heating pipe (18), and the heating pipe (18) is wound on the outer wall of the feeding hole (2).
7. A silicone fluidized bed reactor as set forth in claim 3, wherein: the fan (14) is made of aluminum silicate.
8. A silicone fluidized bed reactor as set forth in claim 3, wherein: the side wall of the air cavity (10) is provided with a plurality of air nozzles (13).
9. A silicone fluidized bed reactor as set forth in claim 3, characterized in that: the inner end side wall of the air cavity (10) is funnel-shaped, and the lower end of the air cavity is fixedly connected with the discharge hole (3).
10. A silicone fluidized bed reactor as set forth in claim 3, characterized in that: the fan blades of the fan (14) are flat rectangles.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210364540.2A CN114653313A (en) | 2022-04-07 | 2022-04-07 | Organosilicon fluidized bed reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210364540.2A CN114653313A (en) | 2022-04-07 | 2022-04-07 | Organosilicon fluidized bed reactor |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN114653313A true CN114653313A (en) | 2022-06-24 |
Family
ID=82035415
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202210364540.2A Pending CN114653313A (en) | 2022-04-07 | 2022-04-07 | Organosilicon fluidized bed reactor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN114653313A (en) |
Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| IT8322642A0 (en) * | 1982-08-31 | 1983-08-25 | Foster Wheeler Energy Corp | FLUID BED REACTOR PLANT. |
| US5627243A (en) * | 1993-12-27 | 1997-05-06 | Borealis Polymers Oy | Fluidized-bed reactor |
| CN203379870U (en) * | 2013-07-05 | 2014-01-08 | 江苏科圣化工机械有限公司 | Organosilicone fluidized bed reactor capable of strengthening gas distribution |
| CN104511262A (en) * | 2013-09-29 | 2015-04-15 | 江苏弘博新材料有限公司 | Organic silicon monomer synthesis fluidized bed reactor |
| US20150217252A1 (en) * | 2012-08-29 | 2015-08-06 | Hemlock Semiconductor Corporation | Taper fluidized bed reactor and process for its use |
| CN206823763U (en) * | 2017-01-03 | 2018-01-02 | 安徽喜宝高分子材料有限公司 | A kind of high-efficiency cold-hot reactor |
| CN208244619U (en) * | 2018-01-19 | 2018-12-18 | 东莞嘉蓝素环保科技有限公司 | A kind of uniformly mixed urea for vehicle standard solution aeration mixing arrangement |
| CN109529731A (en) * | 2018-12-07 | 2019-03-29 | 淮阴工学院 | Organosilicon fluidized bed reactor |
| CN111068602A (en) * | 2019-12-20 | 2020-04-28 | 辽宁新邦新材料有限公司 | Device and method for producing phenylchlorosilane |
| CN215464291U (en) * | 2021-01-31 | 2022-01-11 | 应城市东诚有机硅有限公司 | Reaction tower for continuously producing organic silicon |
-
2022
- 2022-04-07 CN CN202210364540.2A patent/CN114653313A/en active Pending
Patent Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| IT8322642A0 (en) * | 1982-08-31 | 1983-08-25 | Foster Wheeler Energy Corp | FLUID BED REACTOR PLANT. |
| US5627243A (en) * | 1993-12-27 | 1997-05-06 | Borealis Polymers Oy | Fluidized-bed reactor |
| US20150217252A1 (en) * | 2012-08-29 | 2015-08-06 | Hemlock Semiconductor Corporation | Taper fluidized bed reactor and process for its use |
| CN203379870U (en) * | 2013-07-05 | 2014-01-08 | 江苏科圣化工机械有限公司 | Organosilicone fluidized bed reactor capable of strengthening gas distribution |
| CN104511262A (en) * | 2013-09-29 | 2015-04-15 | 江苏弘博新材料有限公司 | Organic silicon monomer synthesis fluidized bed reactor |
| CN206823763U (en) * | 2017-01-03 | 2018-01-02 | 安徽喜宝高分子材料有限公司 | A kind of high-efficiency cold-hot reactor |
| CN208244619U (en) * | 2018-01-19 | 2018-12-18 | 东莞嘉蓝素环保科技有限公司 | A kind of uniformly mixed urea for vehicle standard solution aeration mixing arrangement |
| CN109529731A (en) * | 2018-12-07 | 2019-03-29 | 淮阴工学院 | Organosilicon fluidized bed reactor |
| CN111068602A (en) * | 2019-12-20 | 2020-04-28 | 辽宁新邦新材料有限公司 | Device and method for producing phenylchlorosilane |
| CN215464291U (en) * | 2021-01-31 | 2022-01-11 | 应城市东诚有机硅有限公司 | Reaction tower for continuously producing organic silicon |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101274245B (en) | Annular space air-lift gas-solid loop flow reactor | |
| CN210473928U (en) | High-yield aluminum fluoride synthesis device with multi-stage reaction reflux | |
| CN102350274B (en) | Phenyl fluidized bed reactor | |
| CN114653313A (en) | Organosilicon fluidized bed reactor | |
| CN208223080U (en) | A kind of New Type Vacuum Rake Dryer | |
| CN111777341B (en) | Limestone suspension calcining equipment | |
| CN111203171B (en) | Novel self-pressure forced circulation type reactor for gas-liquid phase reaction | |
| CN218452197U (en) | A stirring crystallization reation kettle for cobalt sulfate production | |
| CN210340356U (en) | Low-energy-consumption multistage reaction reflux aluminum fluoride synthesis device | |
| CN106732290A (en) | A kind of reactor of continuous production nitromethane | |
| CN114923193B (en) | Harmful gas combustion reactor | |
| CN206566900U (en) | A kind of reactor of continuous production nitromethane | |
| JPH0515769A (en) | Chemical reaction device bringing powder and gas into contact with each other | |
| CN213032482U (en) | Ethoxylation reactor | |
| CN214076604U (en) | Reaction kettle | |
| CN106839855A (en) | A kind of fluidized-bed reactor and a kind of heat transmission equipment | |
| CN110773085B (en) | Gas-liquid reactor | |
| CN208200850U (en) | Dry coal powder pressure gasifying system | |
| CN108543506B (en) | Reactor for recovering acetonitrile as by-product in acrylonitrile production process | |
| CN111530407B (en) | Esterification reactor and esterification reaction method | |
| CN217795857U (en) | Second order vertical mixer | |
| CN111167385B (en) | Jet type gas-liquid reactor for preparing acid by utilizing aldehyde raw material and air | |
| CN109225116A (en) | A kind of differential impact flow reactor of sieve pore nozzle | |
| CN221046087U (en) | Reaction device | |
| CN220677801U (en) | Multi-pipe serial continuous reactor for gas-solid two-phase reaction |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20240524 Address after: 838299 West of Kekeya Road, Stone Industrial Park, Shanshan County, Turpan, Xinjiang Uygur Autonomous Region (Hesheng Industrial Park) Applicant after: Xinjiang Hesheng Silicon New Materials Co.,Ltd. Country or region after: China Address before: 241000 room 1202, Yongjin garden, Zhujiang Road, economic and Technological Development Zone, Jiujiang District, Wuhu City, Anhui Province Applicant before: Wu Congrui Country or region before: China |