CN220405627U - Device for continuously producing dibromoethane - Google Patents
Device for continuously producing dibromoethane Download PDFInfo
- Publication number
- CN220405627U CN220405627U CN202321895921.XU CN202321895921U CN220405627U CN 220405627 U CN220405627 U CN 220405627U CN 202321895921 U CN202321895921 U CN 202321895921U CN 220405627 U CN220405627 U CN 220405627U
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- CN
- China
- Prior art keywords
- tail gas
- bromine
- kettle
- dibromoethane
- absorption tank
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- 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.)
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- APQIUTYORBAGEZ-UHFFFAOYSA-N 1,1-dibromoethane Chemical compound CC(Br)Br APQIUTYORBAGEZ-UHFFFAOYSA-N 0.000 title claims abstract description 63
- WKBOTKDWSSQWDR-UHFFFAOYSA-N Bromine atom Chemical compound [Br] WKBOTKDWSSQWDR-UHFFFAOYSA-N 0.000 claims abstract description 94
- GDTBXPJZTBHREO-UHFFFAOYSA-N bromine Substances BrBr GDTBXPJZTBHREO-UHFFFAOYSA-N 0.000 claims abstract description 94
- 229910052794 bromium Inorganic materials 0.000 claims abstract description 94
- 238000010521 absorption reaction Methods 0.000 claims abstract description 83
- 238000011084 recovery Methods 0.000 claims abstract description 70
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 56
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 56
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims abstract description 29
- 239000005977 Ethylene Substances 0.000 claims abstract description 28
- 238000001816 cooling Methods 0.000 claims abstract description 19
- 238000011027 product recovery Methods 0.000 claims abstract description 7
- 239000000463 material Substances 0.000 claims abstract description 3
- 230000005587 bubbling Effects 0.000 claims description 65
- 239000007788 liquid Substances 0.000 claims description 22
- 239000006200 vaporizer Substances 0.000 claims description 4
- 238000010924 continuous production Methods 0.000 claims 5
- 238000004519 manufacturing process Methods 0.000 abstract description 9
- 238000006243 chemical reaction Methods 0.000 description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 6
- 241000197194 Bulla Species 0.000 description 4
- 208000002352 blister Diseases 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 3
- 239000005630 Diquat Substances 0.000 description 2
- SYJFEGQWDCRVNX-UHFFFAOYSA-N diquat Chemical compound C1=CC=[N+]2CC[N+]3=CC=CC=C3C2=C1 SYJFEGQWDCRVNX-UHFFFAOYSA-N 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000002349 favourable effect Effects 0.000 description 2
- 238000000034 method Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- PAAZPARNPHGIKF-UHFFFAOYSA-N 1,2-dibromoethane Chemical compound BrCCBr PAAZPARNPHGIKF-UHFFFAOYSA-N 0.000 description 1
- 230000001174 ascending effect Effects 0.000 description 1
- 230000003139 buffering effect Effects 0.000 description 1
- 229920002678 cellulose Polymers 0.000 description 1
- 239000001913 cellulose Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 210000004400 mucous membrane Anatomy 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000000638 stimulation Effects 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model discloses a device for continuously producing dibromoethane, which comprises a Venturi mixer, a synthesis kettle, a transfer kettle and a tail gas recovery mechanism; the venturi mixer is connected with an ethylene feeding mechanism and a bromine feeding mechanism; the venturi mixer is connected with the synthesis kettle, and a circulating cooling mechanism is arranged between the venturi mixer and the synthesis kettle; the synthesis kettle is connected with the transfer kettle; the materials in the synthesis kettle overflow and then enter the transfer kettle; the ethylene remained in the synthesis kettle enters the transfer kettle; the transfer kettle is connected with a finished product recovery tank; the tail gas recovery mechanism is connected with the transfer kettle and the synthesis kettle and is connected with a tail gas absorption tower and a bromine feeding mechanism; the tail gas recovery mechanism is used for recovering ethylene and bromine and recovering the produced dibromoethane to flow back into the synthesis kettle. The utility model can not gather a large amount of bromine for a long time, thereby improving the safety; the production process is continuously carried out, and the production efficiency is greatly improved.
Description
Technical Field
The utility model relates to the field of dibromoethane production, in particular to a device for continuously producing dibromoethane.
Background
1, 2-dibromoethane is an organic composition, is a colorless transparent liquid, is slightly soluble in water, and is miscible in most organic solvents. Dibromoethane is one of important raw materials for synthesizing diquat dibromosalt, and along with the continuous expansion of the company scale, the dibromoethane becomes a factor for restricting the synthesis of the diquat dibromosalt of the company; in the traditional process, bromine is primed, ethylene is introduced into the bromine for reaction, and a large amount of bromine is gathered together for a long time to react with the ethylene; however, bromine is hard to volatilize and is not easy to trap; at the same time, bromine has strong oxidizing property, and can cause severe reaction and even combustion when contacted with inflammable substances (such as benzene) and organic substances (such as sugar, cellulose and the like); in addition, bromine is toxic and has strong stimulation and corrosion effects on skin and mucous membrane; therefore, the traditional production mode has low safety performance.
Disclosure of Invention
In order to improve the production safety, the utility model provides a device for continuously producing dibromoethane.
The utility model provides a device for continuously producing dibromoethane, which adopts the following technical scheme:
a device for continuously producing dibromoethane comprises a Venturi mixer, a synthesis kettle, a transfer kettle and a tail gas recovery mechanism; the venturi mixer is connected with an ethylene feeding mechanism and a bromine feeding mechanism; the venturi mixer is connected with the synthesis kettle, and a circulating cooling mechanism is arranged between the venturi mixer and the synthesis kettle; the synthesis kettle is connected with the transfer kettle; the materials in the synthesis kettle overflow and then enter the transfer kettle; the ethylene remained in the synthesis kettle enters the transfer kettle; the transfer kettle is connected with a finished product recovery tank; the tail gas recovery mechanism is connected with the transfer kettle and the synthesis kettle and is connected with a tail gas absorption tower and a bromine feeding mechanism; the tail gas recovery mechanism is used for recovering ethylene and bromine and recovering the produced dibromoethane to flow back into the synthesis kettle.
By adopting the technical scheme, the ethylene feeding mechanism and the bromine feeding mechanism respectively and simultaneously provide ethylene and bromine into the Venturi mixer, the ethylene and the bromine are mixed and reacted in the Venturi mixer to generate dibromoethane, the dibromoethane enters the synthesis kettle, heat generated during the reaction of the ethylene and the bromine can be taken away due to the existence of the circulating cooling mechanism, the dibromoethane in the synthesis kettle overflows into the transfer kettle, and finally overflows into the transfer kettle, and the residual ethylene after the reaction sequentially passes through the synthesis kettle and the transfer kettle and finally enters the tail gas recovery mechanism for recovery and absorption, so that the condition that the bromine is gathered for a large amount of time is avoided, and the safety is improved; meanwhile, the production process is continuously carried out, so that the production efficiency is greatly improved.
Optionally, the circulating cooling mechanism comprises a circulating pump and a cooler; the feeding end of the cooler and the bottom of the synthesis kettle are connected with a first circulating pipe; the circulating pump is arranged on the first circulating pipe; the discharge end of the cooler is connected with the Venturi mixer.
Through adopting above-mentioned technical scheme, the bromine of remaining in the synthetic cauldron and the dibromoethane that has produced get back to the synthetic cauldron again after first circulating pipe, cooler, venturi blender under the effect of circulating pump in proper order for synthetic cauldron and venturi blender obtain the cooling, are favorable to improving the security, and the bromine of remaining is got back to in the venturi blender again simultaneously and is reacted, makes the reaction more abundant.
Optionally, the ethylene feed mechanism comprises a vaporizer.
By adopting the technical scheme, the vaporizer converts liquid ethylene into gaseous ethylene, which is beneficial to subsequent full reaction.
Optionally, the bromine feeding mechanism comprises a metering pump.
By adopting the technical scheme, the metering pump effectively controls the entering amount of bromine, and is beneficial to reducing reaction residues.
Optionally, the tail gas recovery mechanism comprises a buffer tank and a three-stage tail gas recovery assembly; the top of the transfer kettle is connected with a recovery air inlet pipe; the other end of the recovery air inlet pipe is connected with the top of the buffer tank; the top of the buffer tank is connected with a buffer air outlet pipe, and the bottom of the buffer tank is connected with a buffer liquid outlet pipe; the other end of the buffer air outlet pipe is connected with the three-stage tail gas recovery component; the other end of the buffer liquid outlet pipe is connected with the top of the synthesis kettle; the three-stage tail gas recovery assembly is connected with the synthesis kettle and is connected with a tail gas absorption tower and a bromine feeding mechanism.
Through adopting above-mentioned technical scheme, the existence of buffer tank makes the tail gas obtain the buffering, is favorable to the tail gas recovery of follow-up tertiary tail gas recovery subassembly, can make volatilized bromine reliquefaction flow back to the synthetic cauldron simultaneously.
Optionally, the tertiary tail gas recovery component comprises a first tail gas bromine bubbling absorption tank, a second tail gas bromine bubbling absorption tank and a tail gas dibromoethane bubbling absorption tank; the bottoms of the first tail gas bromine bubbling absorption tank, the second tail gas bromine bubbling absorption tank and the tail gas dibromoethane bubbling absorption tank are connected with the top of the synthesis kettle through pipelines; the top of the first tail gas bromine bubbling absorption tank is connected with a first recovery air pipe; the other end of the first recovery air pipe extends into the bottom of the second tail gas bromine bubbling absorption tank; the top of the second tail gas bromine bubbling absorption tank is connected with a second recovery air pipe; the other end of the second recovery air pipe extends into the bottom of the tail gas dibromoethane bubbling absorption tank; the tail gas absorption tower is connected with the tail gas dibromoethane bubbling absorption tank; the bromine feeding mechanism is respectively connected with the tops of the second tail gas bromine bubbling absorption tank and the tail gas dibromoethane bubbling absorption tank; and dibromoethane is arranged in the tail gas dibromoethane bubbling absorption tank.
By adopting the technical scheme, the recovery of ethylene tail gas is realized through the first tail gas bromine bubbling absorption tank and the second tail gas bromine bubbling absorption tank, and the dibromoethane in the tail gas dibromoethane bubbling absorption tank is used for absorbing redundant bromine.
Optionally, the first tail gas bromine bubbling absorption tank and the second tail gas bromine bubbling absorption tank are both provided with cooling components.
Through adopting above-mentioned technical scheme, cooling module can cool off first tail gas bromine tympanic bulla absorption jar and second tail gas bromine tympanic bulla absorption jar, takes away the heat that produces when ethylene and bromine both react, improves the security of first tail gas bromine tympanic bulla absorption jar and second tail gas bromine tympanic bulla absorption jar.
Optionally, the synthesis kettle and the transfer kettle are both provided with cooling components.
Through adopting above-mentioned technical scheme, cooling module can cool off synthetic cauldron and transfer cauldron, takes away the heat that produces when ethylene and bromine both react, improves the security of synthetic cauldron and transfer cauldron.
In summary, the beneficial effects of the utility model are as follows:
1. the condition that a large amount of bromine is gathered for a long time can not occur, and the safety is improved.
2. The production process is continuously carried out, and the production efficiency is greatly improved.
Drawings
Fig. 1 is a schematic structural view of the present utility model.
Reference numerals illustrate:
10. a venturi mixer; 11. a feed pipe;
20. a synthesis kettle; 21. a first circulation pipe; 22. a gas flow guide pipe; 23. a first overflow pipe; 24. a first bank of spite;
30. a circulation pump;
40. a cooler; 41. a second circulation pipe;
50. a transfer kettle; 51. recovering an air inlet pipe; 52. a second overflow pipe; 53. a second row of spite;
60. a tail gas recovery mechanism; 61. a buffer tank; 611. a buffer liquid outlet pipe; 612. a buffer air outlet pipe; 62. a first tail gas bromine bubbling absorption tank; 621. a first liquid recovery tube; 622. a first recovery gas pipe; 623. a first recovery liquid inlet pipe; 63. a second tail gas bromine bubbling absorption tank; 631. a second liquid recovery tube; 632. a second recovery gas pipe; 633. a second recovery liquid inlet pipe; 64. tail gas dibromoethane bubbling absorption tank; 641. a third liquid recovery tube; 642. a third recovery pipe;
70. and (5) recycling the pipe.
Detailed Description
The present utility model will be described in further detail with reference to fig. 1.
The application discloses a device for continuously producing dibromoethane, referring to fig. 1, comprising a venturi mixer 10, a synthesis kettle 20, a circulating cooling mechanism, a transfer kettle 50, a tail gas recovery mechanism 60, a tail gas absorption tower and a finished product recovery tank; the venturi mixer 10 is connected with the synthesis kettle 20; the circulation cooling mechanism is used for realizing circulation between the Venturi mixer 10 and the synthesis kettle 20; the tail gas recovery mechanism 60 is respectively connected with the synthesis kettle 20, the transfer kettle 50 and the tail gas absorption tower; the product recovery tank is connected to the transfer pot 50.
Referring to fig. 1, a venturi mixer 10 is connected to an exhaust gas absorption tower and a bromine feeding mechanism; the tail gas absorption tower comprises a vaporizer; the bromine feeding mechanism comprises a metering pump.
Referring to fig. 1, a feed pipe 11 is connected between a discharge end of a venturi mixer 10 and a top of a synthesis kettle 20; the circulation cooling mechanism includes a circulation pump 30 and a cooler 40; a first circulating pipe 21 is connected between the feeding end of the cooler 40 and the bottom of the synthesis kettle 20; the circulation pump 30 is installed on the first circulation pipe 21; a second circulation pipe 41 is connected between the discharge end of the cooler 40 and the feed end of the venturi mixer 10; the cooling medium of the cooler 40 is water.
Referring to fig. 1, a gas flow guide pipe 22 is connected between the top of the synthesis kettle 20 and the top of the transfer kettle 50; a first overflow pipe 23 is connected between the upper side edge of the synthesis kettle 20 and the bottom of the transfer kettle 50; a second overflow pipe 52 is connected to the upper side of the transfer kettle 50; the other end of the second overflow pipe 52 is connected to a finished product recovery tank.
Referring to FIG. 1, a first bank of spite 24 is connected to the bottom of the synthesis tank 20; the bottom of the transfer kettle 50 is connected with a second row of spite 53; the first row 24 and the second row 53 are provided with valves; the other end of the first row of the solar cell 24 and the other end of the second row of the solar cell 53 are connected with the receiving tank; when servicing equipment is required, the contents of the synthesis kettle 20 and transfer kettle 50 may be directed to the receiving tank via the first and second banks of spite 24, 53.
Referring to fig. 1, the exhaust gas recovery mechanism 60 includes a buffer tank 61 and a three-stage exhaust gas recovery assembly; the three-stage tail gas recovery assembly comprises a first tail gas bromine bubbling absorption tank 62, a second tail gas bromine bubbling absorption tank 63 and a tail gas dibromoethane bubbling absorption tank 64; the top of the transfer kettle 50 is connected with a recovery air inlet pipe 51; the other end of the recovery air inlet pipe 51 is connected with the top of the buffer tank 61; a buffer air outlet pipe 612 is connected to the top of the buffer tank 61; the other end of the buffer air outlet pipe 612 passes through the top of the first tail gas bromine bubbling absorption tank 62 and extends into the bottom of the first tail gas bromine bubbling absorption tank 62; a first recovery air pipe 622 is connected to the top of the first tail gas bromine bubbling absorption tank 62; the other end of the first recovery air pipe 622 passes through the top of the second tail gas bromine bubbling absorption tank 63 and extends into the bottom of the second tail gas bromine bubbling absorption tank 63; a second recovery air pipe 632 is connected to the top of the second tail gas bromine bubbling absorption tank 63; the other end of the second recovery gas pipe 632 passes through the top of the tail gas dibromoethane bubbling absorption tank 64 and extends into the bottom of the tail gas dibromoethane bubbling absorption tank 64; a third recovery pipe 642 is connected to the top of the tail gas dibromoethane bubbling absorption tank 64; the other end of the third recovery pipe 642 is connected to the tail gas absorption tower.
Referring to fig. 1, a first recovery liquid inlet pipe 623 is connected to the top of the first tail gas bromine bubbling absorption tank 62; a second recovery liquid inlet pipe 633 is connected to the top of the second tail gas bromine bubbling absorption tank 63; the other end of the first recovery liquid inlet pipe 623 and the other end of the second recovery liquid inlet pipe 633 are connected with a bromine feeding mechanism; the bromine flowing downward in the first off-gas bromine bubbling absorption tank 62 and the second off-gas bromine bubbling absorption tank 63 reacts with the ascending ethylene so that the ethylene is absorbed and dibromoethane is generated, and the off-gas dibromoethane bubbling absorption tank 64 contains dibromoethane and the dibromoethane therein is used for absorbing the excessive bromine.
Referring to fig. 1, a recovery pipe 70 is connected to the top of the synthesis tank 20; a buffer liquid outlet pipe 611 is connected to the bottom of the buffer tank 61; a first liquid recovery pipe 621 is connected to the bottom of the first tail gas bromine bubbling absorption tank 62; a second liquid recovery tube 631 is connected to the bottom of the second tail gas bromine bubbling absorption tank 63; a third liquid recovery tube 641 is connected to the bottom of the tail gas dibromoethane bubbling absorption tank 64; the other end of the first liquid recovery tube 621, the other end of the second liquid recovery tube 631, and the other end of the third liquid recovery tube 641 are all connected to the recovery tube 70.
Referring to fig. 1, cooling components are arranged on the synthesis kettle 20, the transfer kettle 50, the first tail gas bromine bubbling absorption tank 62 and the second tail gas bromine bubbling absorption tank 63; the cooling component comprises a cold water inlet pipe connected to the bottom of the kettle body or the tank body and a cold water outlet pipe connected to the side edge of the upper part of the kettle body or the tank body; a heat exchange device is connected between one ends of the cold water inlet pipe and the cold water outlet pipe, which are far away from the kettle body or the tank body.
The device for continuously producing dibromoethane has the working principle that:
ethylene and bromine enter a Venturi mixer 10 to carry out mixing reaction, so as to generate dibromoethane; dibromoethane is then fed into synthesis tank 20; the circulation cooling mechanism drives dibromoethane and residual bromine in the synthesis kettle 20 to circulate in the venturi mixer 10 and the synthesis kettle 20 and cool the venturi mixer 10, then the dibromoethane overflows into the transfer kettle 50, and then the dibromoethane overflows into the finished product recovery tank; simultaneously, the residual ethylene and the volatilized bromine enter a buffer tank 61 after passing through a transfer tank 50, the volatilized bromine in the buffer tank 61 is liquefied again and flows back to the synthesis tank 20, the ethylene sequentially enters a first tail gas bromine bubbling absorption tank 62 and a second tail gas bromine bubbling absorption tank 63, the ethylene reacts with the bromine entering from a bromine feeding mechanism in the process so as to be absorbed and generate dibromoethane, the dibromoethane finally flows back to the synthesis tank 20, the dibromoethane is filled in a tail gas dibromoethane bubbling absorption tank 64 and is used for absorbing the redundant bromine from the first tail gas bromine bubbling absorption tank 62 and the second tail gas bromine bubbling absorption tank 63, and finally the residual air flow enters a tail gas absorption tower.
The above embodiments are not intended to limit the scope of the present utility model, so: all equivalent changes in structure, shape and principle of the utility model should be covered in the scope of protection of the utility model.
Claims (8)
1. A device for continuously producing dibromoethane, which is characterized in that: comprises a Venturi mixer (10), a synthesis kettle (20), a transfer kettle (50) and a tail gas recovery mechanism (60); the venturi mixer (10) is connected with an ethylene feeding mechanism and a bromine feeding mechanism; the venturi mixer (10) is connected with the synthesis kettle (20) and a circulating cooling mechanism is arranged between the venturi mixer and the synthesis kettle; the synthesis kettle (20) is connected with the transfer kettle (50); the materials in the synthesis kettle (20) overflow and then enter the transfer kettle (50); the ethylene remained in the synthesis kettle (20) enters the transfer kettle (50); the transfer kettle (50) is connected with a finished product recovery tank; the tail gas recovery mechanism (60) is connected with the transfer kettle (50) and the synthesis kettle (20) and is connected with a tail gas absorption tower and a bromine feeding mechanism; the tail gas recovery mechanism (60) is used for recovering ethylene and recovering the dibromoethane produced and flowing the dibromoethane back into the synthesis kettle (20).
2. An apparatus for continuous production of dibromoethane according to claim 1, wherein: the circulating cooling mechanism comprises a circulating pump (30) and a cooler (40); the feeding end of the cooler (40) and the bottom of the synthesis kettle (20) are connected with a first circulating pipe (21); a circulation pump (30) is mounted on the first circulation pipe (21); the discharge end of the cooler (40) is connected with the Venturi mixer (10).
3. An apparatus for continuous production of dibromoethane according to claim 1, wherein: the ethylene feed mechanism includes a vaporizer.
4. An apparatus for continuous production of dibromoethane according to claim 1, wherein: the bromine feeding mechanism comprises a metering pump.
5. An apparatus for continuous production of dibromoethane according to claim 1, wherein: the tail gas recovery mechanism (60) comprises a buffer tank (61) and a three-stage tail gas recovery assembly; the top of the transfer kettle (50) is connected with a recovery air inlet pipe (51); the other end of the recovery air inlet pipe (51) is connected with the top of the buffer tank (61); the top of the buffer tank (61) is connected with a buffer air outlet pipe (612), and the bottom of the buffer tank is connected with a buffer liquid outlet pipe (611); the other end of the buffer air outlet pipe (612) is connected with a three-stage tail gas recovery component; the other end of the buffer liquid outlet pipe (611) is connected with the top of the synthesis kettle (20); the three-stage tail gas recovery assembly is connected with the synthesis kettle (20) and is connected with a tail gas absorption tower and a bromine feeding mechanism.
6. An apparatus for continuously producing dibromoethane according to claim 5, wherein: the three-stage tail gas recovery assembly comprises a first tail gas bromine bubbling absorption tank (62), a second tail gas bromine bubbling absorption tank (63) and a tail gas dibromoethane bubbling absorption tank (64); the bottoms of the first tail gas bromine bubbling absorption tank (62), the second tail gas bromine bubbling absorption tank (63) and the tail gas dibromoethane bubbling absorption tank (64) are connected with the top of the synthesis kettle (20) through pipelines; a first recovery air pipe (622) is connected to the top of the first tail gas bromine bubbling absorption tank (62); the other end of the first recovery air pipe (622) extends into the bottom of the second tail gas bromine bubbling absorption tank (63); the top of the second tail gas bromine bubbling absorption tank (63) is connected with a second recovery air pipe (632); the other end of the second recovery air pipe (632) extends into the bottom of the tail gas dibromoethane bubbling absorption tank (64); the tail gas absorption tower is connected with the tail gas dibromoethane bubbling absorption tank (64); the bromine feeding mechanism is respectively connected with the tops of the second tail gas bromine bubbling absorption tank (63) and the tail gas dibromoethane bubbling absorption tank (64); and dibromoethane is arranged in the tail gas dibromoethane bubbling absorption tank (64).
7. An apparatus for continuously producing dibromoethane according to claim 6, wherein: and cooling components are arranged on the first tail gas bromine bubbling absorption tank (62) and the second tail gas bromine bubbling absorption tank (63).
8. An apparatus for continuous production of dibromoethane according to claim 1, wherein: the synthesis kettle (20) and the transfer kettle (50) are both provided with cooling components.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321895921.XU CN220405627U (en) | 2023-07-18 | 2023-07-18 | Device for continuously producing dibromoethane |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321895921.XU CN220405627U (en) | 2023-07-18 | 2023-07-18 | Device for continuously producing dibromoethane |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN220405627U true CN220405627U (en) | 2024-01-30 |
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ID=89641758
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202321895921.XU Active CN220405627U (en) | 2023-07-18 | 2023-07-18 | Device for continuously producing dibromoethane |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN220405627U (en) |
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2023
- 2023-07-18 CN CN202321895921.XU patent/CN220405627U/en active Active
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