CN201997316U - Fluid bed reactor for preparing chloroethylene - Google Patents
Fluid bed reactor for preparing chloroethylene Download PDFInfo
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- CN201997316U CN201997316U CN201020662932XU CN201020662932U CN201997316U CN 201997316 U CN201997316 U CN 201997316U CN 201020662932X U CN201020662932X U CN 201020662932XU CN 201020662932 U CN201020662932 U CN 201020662932U CN 201997316 U CN201997316 U CN 201997316U
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Abstract
The utility model relates to a fluid bed reactor for preparing chloroethylene, and belongs to a device used in the technology of preparing chloroethylene through the reaction of hydrogen chloride and acetylene. The fluid bed reactor for preparing chloroethylene comprises a reaction tank, wherein a raw material gas inlet and a dead catalyst outlet are formed at the bottom of the reaction tank; a reaction gas outlet and a catalyst inlet are arranged at the upper part of the reaction tank; the reaction tank is internally provided with an upper gas distributor and a lower gas distributor; respective catalyst dense phase areas are formed on the gas distributors; a heat exchange pipe is arranged in each catalyst dense phase area; a lifting pipe is arranged at the outer part of the reaction tank, an upper port of the lifting pipe is connected with the upper catalyst dense phase area, and a lower port of the lifting pipe is connected with the lower catalyst dense phase area; an overflow pipe is arranged at the outer part of the reaction tank and connected with the two catalyst dense phase areas respectively; a mercury removing device and a dust collecting device are arranged on a reaction gas outlet pipe; and a draught fan is arranged on a reaction gas circulation pipe. Due to the fluid bed reactor, the reaction heat is guaranteed to be removed timely, so that the temperature in the reaction tank is lower and uniform.
Description
Technical field
The utility model belongs to hydrogen chloride and acetylene reaction and prepares the device that uses in the technology of vinyl chloride, and what be specifically related to is a kind of fluidized-bed reactor for preparing vinyl chloride.
Background technology
Industrial hydrogen chloride and the acetylene reaction of utilizing prepares vinyl chloride, often adopts fixed-bed column reactor, under the effect of mercury catalyst catalyst, reacts generation vinyl chloride down at 100-180 ℃.Because this reaction is a strong exothermal reaction, this just makes the catalyst granules internal temperature often be higher than the gas phase body temperature, and the heat transfer property of fixed bed reactors is bad, this causes the focus in the reactor to produce, very unfavorable for the heat endurance that keeps mercury catalyst, make the production capacity of fixed bed reactors be subjected to severely restricts, desire enlarges the production capacity of vinyl chloride, the platform number that has only continuous increase fixed bed reactors, but this investment cost that also increases widely.
Summary of the invention
The purpose of this utility model provides a kind of fluidized-bed reactor for preparing vinyl chloride, and it is used to solve the bad problem of heat transfer property that the existing fixed bed that adopts when preparing vinyl chloride with hydrogen chloride and acetylene reaction exists.
The technical scheme that its technical problem that solves the utility model adopts is: the fluidized-bed reactor of this preparation vinyl chloride comprises retort, the bottom of retort is provided with unstrpped gas inlet and dead catalyst outlet, and respond gas vent and catalyst of the top of retort adds inlet; Gas distributor and following gas distributor are set in the retort, form catalyst emulsion zone separately on each gas distributor, in each catalyst emulsion zone heat exchanger tube is installed all; Riser is installed in the retort outside, the upper port of riser links to each other with last catalyst emulsion zone, the lower port of riser links to each other with following catalyst emulsion zone bottom, and overflow pipe is installed in the outside of retort, and overflow pipe links to each other with two catalyst emulsion zones respectively; Mercury removal device and dust arrester are installed on the reacting gas escape pipe, and the reacting gas circulation pipe is installed between reacting gas air inlet pipe and the reacting gas escape pipe, on the reacting gas circulation pipe blower fan is installed.
Gas distributor in the such scheme is the float-valve type distributor.
Distance in the such scheme between last gas distributor and the following gas distributor is 5-8 a times of retort tank diameter.
Distance in the such scheme between the last gas distributor of overflow pipe upper port distance is 2 times of retort tank diameter, and the distance under the overflow pipe lower port distance between the gas distributor is 2 times of retort tank diameter.
The utlity model has following beneficial effect:
1, gas distributor and following gas distributor on the utility model is provided with in retort, form catalyst emulsion zone separately on each gas distributor, in each catalyst emulsion zone heat exchanger tube is installed all, guaranteed in time shifting out of reaction heat, make in the retort temperature lower and even, in addition, two catalyst emulsion zones adopt the alternating temperatures operation during reaction, have than the catalyst emulsion zone of low operating temperature and reaction gas can be lowered the temperature, the mercury that runs off in lower floor's catalyst emulsion zone is captured.
2, the utility model can be beaten portioned product gas circulation and mix with fresh feed gas at retort outer setting blower fan, improves the fluidization quality of two catalyst emulsion zones, has improved the operating flexibility and the conductivity of heat of retort.
Description of drawings
Fig. 1 is a structural representation of the present utility model.
On 1 retort 2 on 3 times gas distributors 4 of gas distributor 5 times catalyst emulsion zone 6 unstrpped gases of catalyst emulsion zone, 7 dead catalyst outlets, 8 heat exchanger tubes, 9 heat exchanger tubes, 10 overflow pipes, 11 risers, 12 reaction gas outlet, 13 catalyst that enter the mouth add inlet 14 blower fans 15 mercury removal devices 16 dust arresters 17 reacting gas circulation pipes 18 reacting gas air inlet pipe 19 reacting gas escape pipes
The specific embodiment
In conjunction with the accompanying drawings the utility model is described further:
As shown in Figure 1, the fluidized-bed reactor of this preparation vinyl chloride has a vertical response jar 1, and the bottom of retort 1 is provided with unstrpped gas inlet 6 and dead catalyst outlet 7, and respond gas vent 12 and catalyst of the top of retort 1 adds inlet 13; Gas distributor 2 and following gas distributor 3 are set in the retort 1, gas distributor is the float-valve type distributor, form catalyst emulsion zone 4 on the last gas distributor 2, form catalyst emulsion zone 5 down on the following gas distributor 3, in the last catalyst emulsion zone 4 heat exchanger tube 8 is installed, in the following catalyst emulsion zone 5 heat exchanger tube 9 is installed also; Riser 11 is installed in retort 1 outside, the upper port of riser 11 links to each other with last catalyst emulsion zone 4, the lower port of riser 11 links to each other with following catalyst emulsion zone 5 bottoms, and overflow pipe 10 is installed in the outside of retort 1, and overflow pipe 10 links to each other with two catalyst emulsion zones respectively; Mercury removal device 15 and dust arrester 16 are installed on the reacting gas escape pipe 19, dust arrester 16 is the plate-type dedusting filter, reacting gas circulation pipe 17 is installed between reacting gas air inlet pipe 18 and the reacting gas escape pipe 19, and blower fan 14 is installed on the reacting gas circulation pipe 17.
Distance in the present embodiment between last gas distributor 2 and the following gas distributor 3 is 6 times of retort 1 tank diameter.Distance between the last gas distributor 2 of overflow pipe 10 upper port distance is 2 times of retort 1 tank diameter, and the distance under the overflow pipe 10 lower port distance between the gas distributor 3 is 2 times of retort 1 tank diameter.
When utilizing the fluidized-bed reactor production vinyl chloride of this preparation vinyl chloride, feed nitrogen or the loosening wind of air conduct from retort 1 bottom unstrpped gas inlet 6, simultaneously catalyst is added inlet 13 retort 1 of packing into from catalyst, make it respectively last, pile up on the following gas distributor and form corresponding catalyst emulsion zone, make the catalyst the retort 1 be in fluidized state from unstrpped gas inlet 6 logical inert gases then, again to heat exchanger tube (8,9) feed the high temperature heat transferring medium in, the temperature of catalyst emulsion zone 5 is elevated to about 125 ℃, the temperature of last catalyst emulsion zone 4 is elevated to 60-100 ℃, feed the gaseous mixture of hydrogen chloride and acetylene subsequently from unstrpped gas inlet 6, the mol ratio of control hydrogen chloride and acetylene is 1.2: 1.After the reaction beginning, the temperature of following catalyst emulsion zone 5 is elevated to about 150 ℃ gradually, about 80 ℃ at this moment of the temperature of last catalyst emulsion zone 4, at this moment, the heat transferring medium of the heat exchanger tube 9 in the following catalyst emulsion zone 5 is switched to cooling medium, and the temperature of catalyst emulsion zone 5 is about 130 ℃ under the control.Product gas flows out from the reaction gas outlet 12 of retort, enter mercury removal device 15 and plate-type dedusting filter, 80% of product gas after the demercuration dedusting enters subsequent separation system, remaining 20% product gas mixes with fresh feed gas after by blower fan 14 superchargings and enters retort 1 once more, to improve the fluidization quality of catalyst emulsion zone.
When conversion of alkyne can not satisfy manufacturing technique requirent, by overflow pipe 10 and riser 11 catalyst in two catalyst emulsion zones is fully circulated, can make conversion of alkyne can satisfy the production needs.
When not circulating when improving conversion of alkyne by catalyst in two catalyst emulsion zones, catalyst is discharged from the dead catalyst outlet 7 of retort, add inlet 13 from catalyst simultaneously and add raw catelyst, the assurance process is carried out continuously.
Claims (4)
1. fluidized-bed reactor for preparing vinyl chloride, it is characterized in that: the fluidized-bed reactor of this preparation vinyl chloride comprises retort (1), the bottom of retort (1) is provided with unstrpped gas inlet (6) and dead catalyst outlet (7), and respond gas vent (12) and catalyst of the top of retort (1) adds inlet (13); Gas distributor (2) and following gas distributor (3) are set in the retort (1), form catalyst emulsion zone separately on each gas distributor, in each catalyst emulsion zone heat exchanger tube is installed all; Riser (11) is installed in retort (1) outside, the upper port of riser (11) links to each other with last catalyst emulsion zone (4), the lower port of riser (11) links to each other with following catalyst emulsion zone (5) bottom, overflow pipe (10) is installed in the outside of retort (1), and overflow pipe (10) links to each other with two catalyst emulsion zones respectively; Mercury removal device (15) and dust arrester (16) are installed on the reacting gas escape pipe (19), reacting gas circulation pipe (17) is installed between reacting gas air inlet pipe (18) and the reacting gas escape pipe (19), and reacting gas circulation pipe (17) is gone up blower fan (14) is installed.
2. the fluidized-bed reactor of preparation vinyl chloride according to claim 1 is characterized in that: described gas distributor is the float-valve type distributor.
3. the fluidized-bed reactor of preparation vinyl chloride according to claim 2 is characterized in that: the 5-8 that the described distance that goes up between gas distributor (2) and the following gas distributor (3) is retort (a 1) tank diameter doubly.
4. the fluidized-bed reactor of preparation vinyl chloride according to claim 2, it is characterized in that: the distance between described overflow pipe (10) the upper port last gas distributor of distance (2) is 2 times of retort (1) tank diameter, and the distance under overflow pipe (10) the lower port distance between the gas distributor (3) is 2 times of retort (1) tank diameter.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201020662932XU CN201997316U (en) | 2010-12-09 | 2010-12-09 | Fluid bed reactor for preparing chloroethylene |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201020662932XU CN201997316U (en) | 2010-12-09 | 2010-12-09 | Fluid bed reactor for preparing chloroethylene |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN201997316U true CN201997316U (en) | 2011-10-05 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201020662932XU Expired - Fee Related CN201997316U (en) | 2010-12-09 | 2010-12-09 | Fluid bed reactor for preparing chloroethylene |
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| Country | Link |
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| CN (1) | CN201997316U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111533639A (en) * | 2020-03-28 | 2020-08-14 | 安徽华塑股份有限公司 | Novel chloroethylene dehydration and purification device |
| CN113617298A (en) * | 2021-06-29 | 2021-11-09 | 中国成达工程有限公司 | Method for producing chloroethylene by acetylene method |
-
2010
- 2010-12-09 CN CN201020662932XU patent/CN201997316U/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111533639A (en) * | 2020-03-28 | 2020-08-14 | 安徽华塑股份有限公司 | Novel chloroethylene dehydration and purification device |
| CN113617298A (en) * | 2021-06-29 | 2021-11-09 | 中国成达工程有限公司 | Method for producing chloroethylene by acetylene method |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C17 | Cessation of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20111005 Termination date: 20111209 |