CN110540206B - Online slag discharging device and method for fluidized bed reactor - Google Patents
Online slag discharging device and method for fluidized bed reactor Download PDFInfo
- Publication number
- CN110540206B CN110540206B CN201810531710.5A CN201810531710A CN110540206B CN 110540206 B CN110540206 B CN 110540206B CN 201810531710 A CN201810531710 A CN 201810531710A CN 110540206 B CN110540206 B CN 110540206B
- Authority
- CN
- China
- Prior art keywords
- fluidized bed
- bed reactor
- slag
- valve
- pipeline
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 239000002893 slag Substances 0.000 title claims abstract description 149
- 238000007599 discharging Methods 0.000 title claims abstract description 77
- 238000000034 method Methods 0.000 title claims abstract description 19
- 239000000463 material Substances 0.000 claims abstract description 44
- 238000006243 chemical reaction Methods 0.000 claims abstract description 16
- 239000007789 gas Substances 0.000 claims description 63
- 239000001257 hydrogen Substances 0.000 claims description 10
- 229910052739 hydrogen Inorganic materials 0.000 claims description 10
- 238000010926 purge Methods 0.000 claims description 7
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 6
- 229910021420 polycrystalline silicon Inorganic materials 0.000 claims description 6
- 238000005984 hydrogenation reaction Methods 0.000 claims description 5
- 229910052757 nitrogen Inorganic materials 0.000 claims description 3
- 125000004435 hydrogen atom Chemical group [H]* 0.000 claims description 2
- 229920005591 polysilicon Polymers 0.000 claims description 2
- 239000013049 sediment Substances 0.000 claims 12
- 208000012839 conversion disease Diseases 0.000 abstract description 3
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 12
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 11
- 239000011863 silicon-based powder Substances 0.000 description 9
- 239000007787 solid Substances 0.000 description 5
- 230000000903 blocking effect Effects 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- VXEGSRKPIUDPQT-UHFFFAOYSA-N 4-[4-(4-methoxyphenyl)piperazin-1-yl]aniline Chemical compound C1=CC(OC)=CC=C1N1CCN(C=2C=CC(N)=CC=2)CC1 VXEGSRKPIUDPQT-UHFFFAOYSA-N 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000005049 silicon tetrachloride Substances 0.000 description 3
- 239000003054 catalyst Substances 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 239000011149 active material Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 230000016507 interphase Effects 0.000 description 1
- 239000012495 reaction gas Substances 0.000 description 1
- 239000011343 solid material Substances 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B33/00—Silicon; Compounds thereof
- C01B33/02—Silicon
- C01B33/021—Preparation
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The invention discloses an online slag discharging device of a fluidized bed reactor and an online slag discharging method, wherein the online slag discharging device comprises a slag receiving tank and a slag discharging pipeline arranged between the fluidized bed reactor and the slag receiving tank, a first valve used for controlling the discharging of the fluidized bed reactor is arranged on the slag discharging pipeline, the online slag discharging device also comprises an air inlet pipeline used for introducing air, the air inlet pipeline is connected with the slag discharging pipeline, and the connecting part of the air inlet pipeline and the slag discharging pipeline is arranged at the downstream of the first valve. And under the condition that the fluidized bed reactor is not stopped, the inactivated materials in the fluidized bed reactor are discharged, the effective reaction material proportion in the fluidized bed reactor is improved, and the reaction conversion rate in the fluidized bed reactor is improved.
Description
Technical Field
The invention belongs to the technical field of polycrystalline silicon production, and particularly relates to an online slag discharging device and an online slag discharging method for a fluidized bed reactor.
Background
In the fluidized bed reactors in the prior art, all fluidized bed reactors are gas-solid fluidized bed reactors, mass transfer, mixing and heat transfer among phases are important indexes for determining the reaction state, and the production yield, the conversion rate and the product quality are directly influenced. For a gas-solid reaction system, interphase mass transfer is often a key factor determining the effect of a fluidized bed reactor.
In the fluidized bed reactor used above, along with the operation of the system, the inactive materials and impurities thereof in the fluidized bed can be continuously accumulated, while the bed layer in the fluidized bed is fixed, the more the inactive materials are accumulated, and the less the active materials participate in the reaction. The general treatment measure of manufacturers is to keep the system continuously running and clean the deactivated materials in the fluidized bed reactor when the system is stopped, and the method has the defects that the longer the continuous running time of the system is, the lower the proportion of the effective reaction materials in the fluidized bed is, the continuous reduction of the conversion rate of the system is caused, and the larger influence is caused on the production.
Disclosure of Invention
The technical problem to be solved by the invention is to provide an online slag discharging device and an online slag discharging method for a fluidized bed reactor, aiming at the defects in the prior art, and the device and the method are used for discharging the inactivated materials in the fluidized bed reactor without stopping the fluidized bed reactor, so as to improve the effective reaction material proportion in the fluidized bed reactor.
The technical scheme adopted for solving the technical problem is to provide an online slag discharging device of a fluidized bed reactor, which comprises a slag receiving tank and a slag discharging pipeline arranged between the fluidized bed reactor and the slag receiving tank, wherein a first valve used for controlling the discharging of the fluidized bed reactor is arranged on the slag discharging pipeline, the online slag discharging device also comprises an air inlet pipeline used for introducing air, the air inlet pipeline is connected with the slag discharging pipeline, and the connecting part of the air inlet pipeline and the slag discharging pipeline is arranged at the downstream of the first valve.
Preferably, the on-line slag discharging device of the fluidized bed reactor further comprises a first check valve arranged on the slag discharging pipeline, and the first check valve is arranged at the downstream of the first valve.
Preferably, the on-line slag discharging device of the fluidized bed reactor further comprises a second valve set arranged on the slag discharging pipeline, and the second valve set is arranged at the downstream of the connection position of the air inlet pipeline and the slag discharging pipeline.
Preferably, the second valve group comprises at least two second valves.
Preferably, the on-line slag discharging device of the fluidized bed reactor further comprises a first check valve arranged on the slag discharging pipeline, the first check valve is arranged at the downstream of the first valve, and the second valve group is arranged at the downstream of the first check valve.
Preferably, a third valve group for controlling the intake of gas is provided on the intake line.
Preferably, the third valve set includes a third valve for opening and closing, and a third check valve disposed downstream of the third valve.
Preferably, the outlet of the slag receiving tank is provided with a slag discharge pipeline of the slag receiving tank, and the slag discharge pipeline of the slag receiving tank is provided with a fourth valve.
Preferably, a slag receiving tank gas outlet is arranged on the slag receiving tank, a fluidized bed reactor gas inlet is arranged on the fluidized bed reactor, a pipeline is arranged between the slag receiving tank gas outlet and the fluidized bed reactor gas inlet, and gas in the slag receiving tank flows into the fluidized bed reactor through the pipeline.
The invention also provides a method for online deslagging by using the online deslagging device, which comprises the following steps:
1) gas is introduced through the gas inlet pipeline to purge the slag discharge pipeline so as to ensure the smoothness of the slag discharge pipeline;
2) and continuously introducing gas into the slag discharging pipeline, opening the first valve, discharging the inactivated materials in the fluidized bed reactor into the slag receiving tank through the slag discharging pipeline, and introducing gas into the slag discharging pipeline to reduce the temperature of the inactivated materials discharged from the fluidized bed reactor, so that the inactivated materials entering the slag discharging pipeline are in a fluidized state, accelerate the discharging speed of the inactivated materials and prevent the inactivated materials from blocking the slag discharging pipeline.
3) And after the discharge of the inactivated materials is finished, closing the first valve, and continuously introducing gas to blow the slag discharge pipeline so as to prevent the inactivated materials discharged from the fluidized bed reactor from blocking the slag discharge pipeline.
Preferably, the pressure of gas introduced into the slag discharge pipeline through the gas inlet pipeline in the steps 1), 2) and 3) is 1.8-2.9 MPa.
Preferably, the reaction carried out in the fluidized bed reactor is a polysilicon cold hydrogenation reaction, and the gas introduced into the gas inlet pipeline is hydrogen. The invention aims at the problem that after a fluidized bed reactor used for the cold hydrogenation reaction of polycrystalline silicon runs for a long time, silicon powder and catalyst which are completely reacted are continuously accumulated at the bottom of the fluidized bed reactor, so that the utilization rate of the silicon powder in the fluidized bed reactor and the actual height of a bed layer are influenced. In order to improve the utilization rate of silicon powder in the fluidized bed reactor, the silicon powder deposited in the fluidized bed reactor and other unreacted solid substances are discharged out of the fluidized bed reactor by online deslagging of the fluidized bed reactor, so that the height of an actual bed layer in the fluidized bed reactor is increased, and the conversion rate of silicon tetrachloride is improved.
Preferably, the method further comprises a step 4) of introducing nitrogen into the slag receiving tank for gas replacement after the step 2), and discharging the deactivated materials through an outlet of the slag receiving tank after the replacement is finished.
The invention provides an on-line slag discharging device and method of a fluidized bed reactor, which are used for discharging inactivated materials in the fluidized bed reactor under the condition that the fluidized bed reactor is not stopped, so that the height of an actual bed layer of a fluidized bed in the fluidized bed reactor is increased, the effective reaction material proportion in the fluidized bed reactor is improved, and the reaction conversion rate in the fluidized bed reactor is improved.
Drawings
FIG. 1 is a schematic configuration diagram of an on-line slag discharging apparatus of a fluidized bed reactor in example 1 of the present invention;
FIG. 2 is a schematic view showing the structure of an on-line slag discharging apparatus of a fluidized bed reactor in example 2 of the present invention;
FIG. 3 is a schematic view showing the structure of an on-line slag discharging apparatus of a fluidized bed reactor in example 3 of the present invention.
In the figure: 1-a fluidized bed reactor; 2-a slag receiving tank; 3-a slag discharge pipeline; 4-a first valve; 5-an air intake line; 6-the connection of the gas inlet pipeline and the slag discharge pipeline; 7-a first check valve; 8-a third valve group; 9-a third valve; 10-a third check valve; 11-a slag discharge line of the slag receiving tank; 12-a fourth valve; 13-a second valve group; 14-a second valve; 15-slag charge receiving tank gas outlet; 16-fluidized bed reactor gas inlet; 17-a pipeline; 18-fifth valve.
Detailed Description
In order to make the technical solutions of the present invention better understood, the present invention will be described in further detail with reference to the accompanying drawings and specific embodiments.
Example 1
As shown in fig. 1, the present embodiment provides an online slag discharging device for a fluidized bed reactor 1, which includes a slag receiving tank 2, and a slag discharging pipeline 3 disposed between the fluidized bed reactor 1 and the slag receiving tank 2, wherein the slag discharging pipeline 3 is provided with a first valve 4 for controlling the discharging of the fluidized bed reactor 1, the online slag discharging device further includes an air inlet pipeline 5 for introducing air, the air inlet pipeline 5 is connected to the slag discharging pipeline 3, and a joint 6 between the air inlet pipeline 5 and the slag discharging pipeline 3 is disposed at the downstream of the first valve 4.
The present embodiment provides an online slag discharging apparatus and method for a fluidized bed reactor 1, which discharge inactivated materials in the fluidized bed reactor 1 without stopping the fluidized bed reactor 1, increase the effective reaction material ratio in the fluidized bed reactor 1, and increase the reaction conversion rate in the fluidized bed reactor 1.
It should be noted that the on-line slag discharge device of the fluidized bed reactor 1 in the present embodiment further includes a first check valve 7 disposed on the slag discharge line 3, and the first check valve 7 is disposed downstream of the first valve 4. The first check valve 7 serves to prevent the deactivated materials from flowing backward into the fluidized-bed reactor 1.
Note that the intake line 5 in the present embodiment is provided with a third valve group 8 for controlling the intake of gas. Specifically, the third valve group 8 in the present embodiment includes 1 third valve 9.
In the present embodiment, the slag discharging line 11 of the slag receiving tank 3 is provided at the outlet of the slag receiving tank 2, and the fourth valve 12 is provided on the slag discharging line 11 of the slag receiving tank 3. The fourth valve 12 is opened to allow the material at the bottom of the slag receiving tank 2 to be discharged.
The embodiment also provides an online slag discharging method using the online slag discharging device, which comprises the following steps:
1) the first valve 4 is closed, the third valve 9 is opened, and the gas is introduced through the gas inlet pipeline 5 to purge the slag discharge pipeline 3 so as to ensure the smoothness of the slag discharge pipeline 3. Specifically, the opening degree of the third valve 9 is adjusted to ensure that the flow rate of the gas introduced through the gas inlet pipeline 5 is 300-1500 Nm3/h。
2) The gas is continuously introduced into the slag discharge line 3, the first valve 4 is opened, the deactivated materials in the fluidized bed reactor 1 are discharged into the slag charge receiving tank 2 through the slag discharge line 3, and the temperature of the deactivated materials discharged from the fluidized bed reactor 1 can be reduced by introducing the gas into the slag discharge line 3. Specifically, the flow rate of the discharged deactivated materials in the fluidized bed reactor 1 is 200-2000 kg/h by adjusting the opening degree of the first valve 4.
3) After the discharge of the deactivated materials is finished, the first valve 4 is closed, and gas is continuously introduced to purge the slag discharge pipeline 3, so that the deactivated materials discharged from the fluidized bed reactor 1 are prevented from blocking the slag discharge pipeline 3. Specifically, the opening degree of the third valve 9 is adjusted to ensure that the flow rate of the gas introduced through the gas inlet pipeline 5 is 300-1500 Nm3/h。
Example 2
As shown in fig. 2, the present embodiment provides an online slag discharging device of a fluidized bed reactor 1, which is different from the online slag discharging device in embodiment 1 in that:
the on-line slag discharging device of the fluidized bed reactor 1 in the present embodiment further includes a second valve group 13 disposed on the slag discharging line 3, the second valve group 13 being disposed downstream of the junction 6 of the gas inlet line 5 and the slag discharging line 3, the second valve group 13 being disposed downstream of the first check valve 7. The second valve group 13 is used for controlling the opening and closing of the inlet of the slag receiving tank 2.
It should be noted that the connection 6 between the intake line 5 and the slag discharge line 3 in the present embodiment is disposed on the slag discharge line 3 between the first valve 4 and the second valve group 13, and the second valve group 13 includes two second valves 14. The hydrogen gas introduced into the reject line 3 through the gas inlet line 5 can purge the reject line 3 between the first valve 4 and the second valve group 13. The second valve group 13 comprises two second valves 14, when one second valve 14 fails, the other second valve 14 can still be used, and the safety and reliability of the whole online slag discharge device are improved.
The third valve group 8 in the present embodiment includes a third valve 9 for opening and closing, and a third check valve 10 disposed downstream of the third valve 9. The third check valve 10 serves to prevent the reverse flow of hydrogen gas.
It should be noted that in the present embodiment, the slag receiving tank 2 is provided with a slag receiving tank gas outlet 15, the fluidized bed reactor 1 is provided with a fluidized bed reactor gas inlet 16, a pipeline 17 is provided between the slag receiving tank gas outlet 15 and the fluidized bed reactor gas inlet 16, and the gas in the slag receiving tank 2 flows into the fluidized bed reactor 1 through the pipeline 17. In particular, a fifth valve 18 is arranged on a line 17 between the slag receiving tank gas outlet 15 and the fluidized bed reactor gas inlet 16. A slag receiving tank gas outlet 15 is arranged at the top of the slag receiving tank 2, and a fluidized bed reactor gas inlet 16 is arranged at the bottom of the fluidized bed reactor 1. After the gas in the slag receiving tank 2 flows into the fluidized bed reactor 1, the solid material in the fluidized bed reactor 1 is favorably formed into a fluidized state.
The embodiment also provides a method for carrying out online deslagging by using the online deslagging device, wherein the reaction carried out in the fluidized bed reactor 1 is a cold hydrogenation reaction of polycrystalline silicon, and the method comprises the following steps:
1) and closing the first valve 4, opening the third valve 9, the third check valve 10, the second valve group 13 and the fifth valve 18, and introducing 1.8-2.9 MPa of hydrogen through the air inlet pipeline 5 to purge the slag discharge pipeline 3 so as to ensure the smoothness of the slag discharge pipeline 3. In particular, by adjusting the opening of the third valve 9, so that the air is drawn through the intake line5 the flow rate of the introduced hydrogen is 300-1500 Nm3/h。
2) Continuously introducing 1.8-2.9 MPa of hydrogen into the slag discharge pipeline 3, opening the first valve 4, discharging the deactivated materials in the fluidized bed reactor 1 into the slag receiving tank 2 through the slag discharge pipeline 3, and introducing the hydrogen into the slag discharge pipeline 3 to reduce the temperature of the deactivated materials discharged from the fluidized bed reactor 1 from 400-450 ℃ to 180-250 ℃, so that the deactivated silicon powder entering the slag discharge pipeline 3 is in a fluidized state, the discharge speed of the deactivated silicon powder is accelerated, and the slag discharge pipeline 3 is prevented from being blocked by the deactivated silicon powder. Specifically, the flow rate of the discharged deactivated materials in the fluidized bed reactor 1 is 200-2000 kg/h by adjusting the opening degree of the first valve 4.
3) And after the discharge of the inactivated materials is finished, closing the first valve 4, and continuously introducing 1.8-2.9 MPa of hydrogen to purge the slag discharge pipeline 3 so as to prevent the inactivated materials discharged from the fluidized bed reactor 1 from blocking the slag discharge pipeline 3. Specifically, the opening degree of the third valve 9 is adjusted to ensure that the flow of the hydrogen introduced through the air inlet pipeline 5 is 300-1500 Nm3H is used as the reference value. In the steps 1), 2) and 3), hydrogen is continuously introduced into the slag discharging pipeline 3 through the gas inlet pipeline 5, and the gas flows into the fluidized bed reactor 1 as reaction gas after passing through the slag receiving tank 2, so that the introduced hydrogen is recycled, and the excessive pressure in the slag receiving tank 2 in the online slag discharging process can be prevented.
4) And closing the third valve group 8, the second valve group 13 and the fifth valve 18, introducing nitrogen into the slag receiving tank 2 for gas replacement, and opening the fourth valve 12 after the replacement is finished to discharge the inactivated materials in the slag receiving tank 3.
In the embodiment, after the fluidized bed reactor 1 used for the cold hydrogenation reaction of polycrystalline silicon runs for a long time, silicon powder and catalyst which are completely reacted are continuously accumulated at the bottom of the fluidized bed reactor 1, and the utilization rate of the silicon powder in the fluidized bed reactor 1 and the actual height of a bed layer are influenced. In order to improve the utilization rate of silicon powder in the fluidized bed reactor 1, in this embodiment, the silicon powder deposited in the fluidized bed reactor 1 and other unreacted solid substances are discharged out of the fluidized bed reactor 1 by discharging slag on line from the fluidized bed reactor 1, so as to increase the height of the actual bed layer in the fluidized bed reactor 1 and improve the conversion rate of silicon tetrachloride.
In the embodiment, silicon powder and other unreacted solid substances deposited in the fluidized bed reactor 1 are discharged out of the fluidized bed reactor 1 by online deslagging of the fluidized bed reactor 1, so that the height of an actual bed layer in the fluidized bed reactor 1 is increased, and the conversion rate of silicon tetrachloride is improved.
Example 3
As shown in fig. 3, the present embodiment provides an online slag discharging device of a fluidized bed reactor 1, which is different from the online slag discharging device in embodiment 1 in that:
the connection 6 of the intake line 5 and the discharge line 3 in this embodiment is provided on the discharge line 3 between the first check valve 7 and the second valve group 13. The first check valve 7 can prevent not only the inactivated material in the slag discharge line 3 from flowing back into the fluidized bed reactor 1 but also the hydrogen gas introduced into the slag discharge line 3 through the gas inlet line 5 from flowing back into the fluidized bed reactor 1.
It will be understood that the above embodiments are merely exemplary embodiments taken to illustrate the principles of the present invention, which is not limited thereto. It will be apparent to those skilled in the art that various modifications and improvements can be made without departing from the spirit and substance of the invention, and these modifications and improvements are also considered to be within the scope of the invention.
Claims (10)
1. The utility model provides a fluidized bed reactor's row sediment device on line, including the sediment material receiving tank, the row's sediment pipeline that sets up between fluidized bed reactor and sediment material receiving tank, be provided with the first valve that is used for controlling fluidized bed reactor row material on the row's sediment pipeline, arrange the sediment device on line and still including the pipeline of admitting air that is used for letting in gas, admit air pipeline and arrange the sediment pipe connection, admit air pipeline and arrange the junction of sediment pipeline and set up in the low reaches of first valve, it receives a jar gas outlet to be provided with the sediment material on the sediment material receiving tank, be provided with fluidized bed reactor gas inlet on the fluidized bed reactor, be provided with the pipeline between sediment material receiving tank gas outlet and the fluidized bed reactor gas inlet, the gas in the sediment material receiving tank flows into fluidized bed reactor.
2. The on-line slag discharge apparatus of a fluidized bed reactor according to claim 1, further comprising a first check valve disposed on the slag discharge line, the first check valve being disposed downstream of the first valve.
3. The on-line slag discharge apparatus of a fluidized bed reactor according to claim 1, further comprising a second valve group provided on the slag discharge line, the second valve group being provided downstream of a junction of the gas inlet line and the slag discharge line.
4. The on-line slag discharging device of a fluidized bed reactor according to claim 3, further comprising a first check valve disposed on the slag discharging line, the first check valve being disposed downstream of the first valve, and the second valve group being disposed downstream of the first check valve.
5. The on-line slag discharging device of a fluidized bed reactor according to claim 1, wherein a third valve group for controlling gas feeding is provided on the gas feeding line.
6. The on-line slag discharging device of a fluidized bed reactor according to claim 5, wherein the third valve set comprises a third valve for opening and closing, and a third check valve disposed downstream of the third valve.
7. An online slag discharging method using the online slag discharging device according to any one of claims 1 to 6, comprising the steps of:
1) gas is introduced through the gas inlet pipeline to purge the slag discharge pipeline;
2) continuously introducing gas into the slag discharging pipeline, opening the first valve, and discharging the inactivated materials in the fluidized bed reactor into the slag receiving tank through the slag discharging pipeline;
3) and after the discharge of the inactivated materials is finished, closing the first valve, and continuously introducing gas to blow the slag discharge pipeline.
8. The method for online deslagging according to claim 7, wherein the pressure of gas introduced into the deslagging pipeline through the gas inlet line in the steps 1), 2) and 3) is 1.8-2.9 MPa.
9. The method for discharging slag on line according to claim 7 or 8, characterized in that the reaction carried out in the fluidized bed reactor is a polysilicon cold hydrogenation reaction, and the gas introduced into the gas inlet pipeline is hydrogen.
10. The method for discharging the slag online according to claim 9, wherein the step 2) is followed by a step 4) of introducing nitrogen into the slag receiving tank for gas replacement, and after the replacement is finished, the deactivated materials in the slag receiving tank are discharged through an outlet of the slag receiving tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810531710.5A CN110540206B (en) | 2018-05-29 | 2018-05-29 | Online slag discharging device and method for fluidized bed reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810531710.5A CN110540206B (en) | 2018-05-29 | 2018-05-29 | Online slag discharging device and method for fluidized bed reactor |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN110540206A CN110540206A (en) | 2019-12-06 |
| CN110540206B true CN110540206B (en) | 2021-05-11 |
Family
ID=68700929
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201810531710.5A Active CN110540206B (en) | 2018-05-29 | 2018-05-29 | Online slag discharging device and method for fluidized bed reactor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN110540206B (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114272857B (en) * | 2021-12-31 | 2022-10-28 | 合盛硅业股份有限公司 | Method and system for replacing synthetic organic silicon monomer raw material |
Citations (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN85200147U (en) * | 1985-04-01 | 1986-02-19 | 南京工学院 | Residue extractional device for pressure fluidizing furnace |
| US6344578B1 (en) * | 2000-08-10 | 2002-02-05 | Wacker-Chemie Gmbh | Process for working up residues from the direct synthesis of organochlorosilanes |
| CN1405277A (en) * | 2002-09-27 | 2003-03-26 | 中国科学院山西煤炭化学研究所 | Solid slag-discharing dry-powder air-current bed gasification process and apparatus |
| CN101279735A (en) * | 2008-05-30 | 2008-10-08 | 中蓝晨光化工研究院有限公司 | Production method and apparatus for trichlorosilane |
| CN101942344A (en) * | 2010-09-20 | 2011-01-12 | 中国科学院山西煤炭化学研究所 | Method and device for gasifying multi-segment staged converted fluidized bed |
| CN102745691A (en) * | 2012-07-16 | 2012-10-24 | 特变电工新疆硅业有限公司 | Method and device for recovering waste silicon powder from trichlorosilane synthetic furnace |
| CN105885950A (en) * | 2016-05-20 | 2016-08-24 | 北京化工大学 | Three-bed combination pyrolysis gasification and tar cracking integrated system for solid waste |
| CN106915747A (en) * | 2015-12-28 | 2017-07-04 | 新特能源股份有限公司 | A kind of trichlorosilane synthesis method and device |
| CN104860317B (en) * | 2015-05-18 | 2017-07-21 | 中国化学赛鼎宁波工程有限公司 | The equipment that a kind of cold hydrogenization method prepares trichlorosilane |
| CN206556006U (en) * | 2017-02-17 | 2017-10-13 | 武汉凯迪电力工程有限公司 | A kind of anti-block apparatus of CFBB side wall slag-drip opening |
| CN107337211A (en) * | 2016-05-03 | 2017-11-10 | 新特能源股份有限公司 | The gasification method and vapourizing unit of silicon tetrachloride in a kind of polysilicon cold hydrogenization method |
| CN105776223B (en) * | 2014-12-16 | 2018-02-16 | 新特能源股份有限公司 | Trichlorosilane synthetic furnace and system, the Slagoff method using the synthetic furnace or system |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN202390211U (en) * | 2011-09-19 | 2012-08-22 | 上海森松化工成套装备有限公司 | Hydrogenated silicon tetrachloride fluidized bed reactor |
-
2018
- 2018-05-29 CN CN201810531710.5A patent/CN110540206B/en active Active
Patent Citations (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN85200147U (en) * | 1985-04-01 | 1986-02-19 | 南京工学院 | Residue extractional device for pressure fluidizing furnace |
| US6344578B1 (en) * | 2000-08-10 | 2002-02-05 | Wacker-Chemie Gmbh | Process for working up residues from the direct synthesis of organochlorosilanes |
| CN1405277A (en) * | 2002-09-27 | 2003-03-26 | 中国科学院山西煤炭化学研究所 | Solid slag-discharing dry-powder air-current bed gasification process and apparatus |
| CN101279735A (en) * | 2008-05-30 | 2008-10-08 | 中蓝晨光化工研究院有限公司 | Production method and apparatus for trichlorosilane |
| CN101942344A (en) * | 2010-09-20 | 2011-01-12 | 中国科学院山西煤炭化学研究所 | Method and device for gasifying multi-segment staged converted fluidized bed |
| CN102745691A (en) * | 2012-07-16 | 2012-10-24 | 特变电工新疆硅业有限公司 | Method and device for recovering waste silicon powder from trichlorosilane synthetic furnace |
| CN105776223B (en) * | 2014-12-16 | 2018-02-16 | 新特能源股份有限公司 | Trichlorosilane synthetic furnace and system, the Slagoff method using the synthetic furnace or system |
| CN104860317B (en) * | 2015-05-18 | 2017-07-21 | 中国化学赛鼎宁波工程有限公司 | The equipment that a kind of cold hydrogenization method prepares trichlorosilane |
| CN106915747A (en) * | 2015-12-28 | 2017-07-04 | 新特能源股份有限公司 | A kind of trichlorosilane synthesis method and device |
| CN107337211A (en) * | 2016-05-03 | 2017-11-10 | 新特能源股份有限公司 | The gasification method and vapourizing unit of silicon tetrachloride in a kind of polysilicon cold hydrogenization method |
| CN105885950A (en) * | 2016-05-20 | 2016-08-24 | 北京化工大学 | Three-bed combination pyrolysis gasification and tar cracking integrated system for solid waste |
| CN206556006U (en) * | 2017-02-17 | 2017-10-13 | 武汉凯迪电力工程有限公司 | A kind of anti-block apparatus of CFBB side wall slag-drip opening |
Non-Patent Citations (2)
| Title |
|---|
| "A review of some operation and maintenance issues of CFBC boilers";Anand Arjunwadkar et al;《Applied Thermal Engineering》;20160402;第102卷;第672-694页 * |
| "循环流化床排渣系统的研究和改进";丁晓白 等;《电力学报》;20030715;第18卷(第4期);第260-262页 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN110540206A (en) | 2019-12-06 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| JP4769873B2 (en) | Molten iron manufacturing method with improved charging and discharging of fine iron ore and molten iron manufacturing apparatus using the same | |
| CN110540206B (en) | Online slag discharging device and method for fluidized bed reactor | |
| CN105694959A (en) | Jet-type internal circulation flow reactor for heavy oil hydrocracking | |
| WO2021159790A1 (en) | Petroleum hydrocracking reaction apparatus | |
| CN111320203B (en) | Device and method for improving operation rate of chlorination system | |
| CN105776223B (en) | Trichlorosilane synthetic furnace and system, the Slagoff method using the synthetic furnace or system | |
| JPS6325495A (en) | Generator for streamline flow for transfer line heat exchanger | |
| CN107362765A (en) | Oximation reaction feeding regulating device and adjusting method | |
| CN107227383B (en) | The suppressing method of defluidization is cohered during a kind of pressurized fluidization reduced iron miberal powder | |
| CN111170822A (en) | Process for preparing propylene by propane dehydrogenation in superimposed on-line switchable fluid bed | |
| CN208098029U (en) | Dehydrogenating propane device | |
| CN105779013B (en) | A kind of cold slag system for pressurize gentle air flow bed or fluidized bed coal gasification process | |
| CN108144556A (en) | A kind of boiling bed hydrogenation reaction system and boiling bed hydrogenation technique method | |
| CN105084313B (en) | Method and apparatus for executing CO transformation | |
| CN207929185U (en) | A kind of boiling bed hydrogenation reaction system | |
| CN214496206U (en) | Slag discharging device and gasification system | |
| CN214781945U (en) | Self-heating gas-based shaft furnace direct reduction device | |
| CN211601582U (en) | System for accelerating temperature reduction of shift converter | |
| CN204824190U (en) | Gaseous metallic impurity's of desorption chlorosilane device and have its silicon production system | |
| CN219024231U (en) | Disproportionation device reactor feeding system | |
| CN103528055A (en) | Pressurized ash residue treatment technology and system | |
| CN217541640U (en) | Purging system for powder attached to pipe wall of heat exchanger | |
| CN217568761U (en) | Reaction unit suitable for production high-quality inorganic salt | |
| CN212492845U (en) | Novel fixed bed reactor | |
| JPH02279512A (en) | Production of high-purity polycrystal silicon |
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 | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| EE01 | Entry into force of recordation of patent licensing contract | ||
| EE01 | Entry into force of recordation of patent licensing contract |
Application publication date: 20191206 Assignee: Xinte silicon based new materials Co.,Ltd. Assignor: XINTE ENERGY Co.,Ltd. Contract record no.: X2022990000325 Denomination of invention: On line slag discharging device and method of fluidized bed reactor Granted publication date: 20210511 License type: Common License Record date: 20220627 Application publication date: 20191206 Assignee: Inner Mongolia Xinte silicon material Co.,Ltd. Assignor: XINTE ENERGY Co.,Ltd. Contract record no.: X2022990000326 Denomination of invention: On line slag discharging device and method of fluidized bed reactor Granted publication date: 20210511 License type: Common License Record date: 20220627 |