CN210356338U - Hydrogen peroxide solution oxidation tail gas aromatic separation recovery unit - Google Patents
Hydrogen peroxide solution oxidation tail gas aromatic separation recovery unit Download PDFInfo
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- CN210356338U CN210356338U CN201920942406.XU CN201920942406U CN210356338U CN 210356338 U CN210356338 U CN 210356338U CN 201920942406 U CN201920942406 U CN 201920942406U CN 210356338 U CN210356338 U CN 210356338U
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Abstract
A hydrogen peroxide oxidation tail gas aromatic hydrocarbon separation and recovery device comprises a separation tank, wherein a coalescer and a flow guide pipe are arranged in the separation tank, the coalescer divides the inner space of the separation tank into an upper part and a lower part, the flow guide pipe is arranged on the lower part of the separation tank, the air inlet of the flow guide pipe is arranged at the outer end of the separation tank, a pipeline at the air inlet end is parallel to the coalescer to the center of the separation tank, the air outlet of the flow guide pipe is arranged at the bottom of the separation tank, and a pipeline at the air outlet end is vertical to the coalescer and is intersected and communicated with the; the top end of the upper part of the separation tank is provided with an exhaust port, and the bottom of the upper part of the separation tank is provided with a second liquid outlet; a first liquid discharge port is formed in the bottom of the lower part of the separation tank; simple structure practices thrift the cost, can prolong tail gas rise time, makes the sedimentation separation more abundant effective.
Description
Technical Field
The utility model relates to a chemical industry industrial waste gas separation recovery technical field, in particular to hydrogen peroxide solution oxidation tail gas aromatic separation recovery unit.
Background
In the oxidation process in hydrogen peroxide production, oxygen in the air is used as an oxidant, and a large amount of oxidation tail gas is generated after reaction, wherein the components of the oxidation tail gas are nitrogen, oxygen, trace heavy aromatic hydrocarbon, water and the like, and although the content of the heavy aromatic hydrocarbon is very low, if the heavy aromatic hydrocarbon is not recovered, a large amount of heavy aromatic hydrocarbon is lost; taking a 20 ten thousand tons/year device as an example, the content of aromatic hydrocarbon directly discharged from the oxidation tower is 10-15g/Nm, the discharge amount of the oxidation tower is about 30000 Nm/h, the discharge amount of heavy aromatic hydrocarbon is at least 2400 t/year according to 8000h operation time/year, and the discharge amount of aromatic hydrocarbon is equivalent to 1440 tens of thousands/year loss according to 0.6 ten thousands/t.
At present, heavy aromatics in the oxidized tail gas are usually recovered by adopting a water cooling, cold box, turbine refrigeration and carbon fiber adsorption mode, the recovery rate of the aromatics can reach about 90-95%, more heavy aromatics can not be recovered, and the larger the device is, the lower the recovery efficiency is, and the higher the energy consumption is; the main reason is that: although the temperature after turbine refrigeration can reach 0-5 ℃, the subsequent device adopts natural sedimentation plus an aromatic hydrocarbon of a demister for recovery, the device of the principle is greatly influenced by the flow rate and the retention time of gas, and after the device is increased to a certain degree, the size of a separation device cannot be strictly designed according to the design specification due to the reasons of floor height and the like, so that the larger the device is, the poorer the recovery effect is; the pre-recovery can not achieve a good recovery effect, so that the adsorption recovery effect of the rear-end carbon fibers is influenced, and the energy consumption of the carbon fibers is greatly increased.
For the above problems, at present, a coalescer is added in a separation device of natural sedimentation and a demister, and the coalescer is arranged at the lower end of the demister so as to improve the effect of pre-separation; it has two problems, however: 1. after the heavy aromatic hydrocarbon is coalesced by the coalescer, the granularity of the heavy aromatic hydrocarbon reaches the gravity settling degree, and a demister is not needed; 2. after the tail gas enters the separation, no guide pipe is arranged, the retention time is short, and the natural settling separation effect is poor.
Disclosure of Invention
The utility model aims at overcoming the defects in the prior art, and provides a hydrogen peroxide oxidized tail gas and aromatic hydrocarbon separation and recovery device which has the advantages of simple structure, cost saving, tail gas rising time prolonging, and more sufficient and effective sedimentation separation.
The technical scheme of the utility model lies in: a hydrogen peroxide oxidation tail gas aromatic hydrocarbon separation and recovery device comprises a separation tank, wherein a coalescer and a flow guide pipe are arranged in the separation tank, the coalescer divides the inner space of the separation tank into an upper part and a lower part, the flow guide pipe is arranged on the lower part of the separation tank, the air inlet of the flow guide pipe is arranged at the outer end of the separation tank, a pipeline at the air inlet end is parallel to the coalescer to the center of the separation tank, the air outlet of the flow guide pipe is arranged at the bottom of the separation tank, and a pipeline at the air outlet end is vertical to the coalescer and is intersected and communicated with the;
the top end of the upper part of the separation tank is provided with an exhaust port, and the bottom of the upper part of the separation tank is provided with a second liquid outlet; the bottom of the lower part of the separation tank is provided with a first liquid discharge port.
The upper part of the separation tank is also provided with a second liquid level meter for observing the liquid level in the upper part of the separation tank.
The lower part of the separation tank is also provided with a first liquid level meter for observing the liquid level in the lower part of the separation tank.
The first drainage port is provided with a first drainage pipeline, and the first drainage pipeline is further provided with a first drainage valve.
And a second liquid discharge pipeline is arranged on the second liquid discharge port, and a second liquid discharge valve is further arranged on the second liquid discharge pipeline.
And a through hole matched with the flow guide pipe is formed in the lower part of the separation tank.
The utility model has the advantages that: compared with the prior art, the utility model has novel design and simple structure, and can extend the rising time of the tail gas by entering the bottom of the separation tank through the guide pipe, so that the sedimentation separation is more sufficient and effective, and the separation and recovery effect of the device is further improved; meanwhile, a demister is omitted behind the coalescer, the structure of the device is simplified, the separation and recovery effects are improved, and meanwhile, the cost of the device is reduced.
Drawings
Fig. 1 is a schematic structural diagram of the present invention;
in the figure: 1. the device comprises an air inlet, 2, a flow guide pipe, 3, a first liquid discharge port, 4, a second liquid discharge pipeline, 5, a second liquid discharge port, 6, a coalescer, 7, an air outlet, 8, a second liquid discharge valve, 9, a first liquid discharge valve, 10, a first liquid level meter, 11, a second liquid level meter, 12, a separation tank, 13 and a first liquid discharge pipeline.
Detailed Description
The technical solution in the embodiments of the present invention will now be clearly and completely described with reference to the accompanying drawings, which are simplified schematic drawings and only schematically illustrate the basic structure of the present invention.
As shown in fig. 1, the utility model comprises a separation tank 12, an air inlet 1, a draft tube 2, a first liquid discharge port 3, a first liquid discharge valve 9, a coalescer 6, a second liquid discharge port 5, a second liquid discharge valve 8, a device exhaust port 7, a first liquid level meter 10, a second liquid level meter 11, a first liquid discharge pipeline 13 and a second liquid discharge pipeline 4; the coalescer 6 and the flow guide pipe 3 are arranged in the device shell 12, the coalescer 6 divides the inner space of the device shell 12 into an upper part and a lower part, the flow guide pipe 2 is arranged on the lower part of the separation tank 12, the air inlet 1 of the flow guide pipe 2 is arranged at the outer end of the separation tank 12, a pipeline at the air inlet end is parallel to the coalescer 6 and is arranged at the center of the separation tank (12), the air outlet of the flow guide pipe 2 is arranged at the bottom of the separation tank 12, the pipeline at the air outlet end is vertical to the coalescer 6 and is intersected and communicated with the pipeline at the air inlet end, and the pipeline enters the bottom of the separation tank through the flow guide pipe, so that the rising time of tail gas; an exhaust port 7 is arranged at the top end of the upper part of the separation tank 12, and a second liquid outlet 5 is arranged at the bottom of the upper part of the separation tank 12; the bottom of the lower part of the separation tank 12 is provided with a first liquid discharge port 3; the first drain valve 9 is connected with the first drain port 3 through a first drain pipeline 13, and the second drain valve 8 is connected with the second drain port 5 through a second drain pipeline 4; the first liquid level meter 10 is arranged on the lower part of the separation tank 12, and the second liquid level meter 11 is arranged on the upper half part of the separation tank 12; the utility model has novel design and simple structure, and omits a demister behind the coalescer, thereby simplifying the structure of the device and reducing the cost of the device;
the tail gas flows in the device:
hydrogen peroxide oxidation tail gas enters the flow guide pipe 2 from the gas inlet 1, gas enters the bottom of the separation tank 12 along with the flow guide pipe 2, the tail gas rises from the bottom of the separation tank 12 to flow to the coalescer 6, and finally the tail gas is discharged from the gas outlet 7 of the device.
And (3) discharging heavy aromatics separated from tail gas from the device:
through first liquid level gauge 10, observe the heavy aromatics 'of knockout drum 12 the latter half natural settling separation recovery's volume, after reaching certain degree, open first blow-off valve 9, discharge heavy aromatics from first drain outlet 3.
The amount of heavy aromatic hydrocarbons recovered by the upper half coalescer 6 of the separation tank 12 was observed by the second level gauge 11, and when a certain amount of heavy aromatic hydrocarbons was recovered, the second drain valve 8 was opened to drain the heavy aromatic hydrocarbons from the second drain port 5.
Claims (6)
1. The utility model provides a hydrogen peroxide solution oxidation tail gas arene separation recovery unit which characterized in that: the separator comprises a separation tank (12), wherein a coalescer (6) and a flow guide pipe (2) are installed in the separation tank (12), the coalescer (6) divides the inner space of the separation tank (12) into an upper part and a lower part, the flow guide pipe (2) is installed on the lower part of the separation tank (12), an air inlet (1) of the flow guide pipe (2) is arranged at the outer end of the separation tank (12), a pipeline at the air inlet end is parallel to the coalescer (6) to the center of the separation tank (12), an air outlet of the flow guide pipe (2) is arranged at the bottom of the separation tank (12), and a pipeline at the air outlet end is vertical to the coalescer (6) and is intersected and communicated with the pipeline at the air inlet;
an exhaust port (7) is arranged at the top end of the upper part of the separation tank (12), and a second liquid outlet (5) is arranged at the bottom of the upper part of the separation tank (12); the bottom of the lower part of the separating tank (12) is provided with a first drainage port (3).
2. The separation and recovery device for aromatic hydrocarbons in hydrogen peroxide oxidized tail gas according to claim 1, characterized in that: the upper part of the separation tank (12) is also provided with a second liquid level meter (11) for observing the liquid level in the upper part of the separation tank (12).
3. The separation and recovery device for aromatic hydrocarbons in hydrogen peroxide oxidized tail gas according to claim 1, characterized in that: the lower part of the separation tank (12) is also provided with a first liquid level meter (10) for observing the liquid level in the lower part of the separation tank (12).
4. The separation and recovery device for aromatic hydrocarbons in hydrogen peroxide oxidized tail gas according to claim 1, characterized in that: install a first drainage pipeline (13) on first drainage mouth (3), still be provided with a first drainage valve (9) on first drainage pipeline (13).
5. The separation and recovery device for aromatic hydrocarbons in hydrogen peroxide oxidized tail gas according to claim 1, characterized in that: and a second liquid discharge pipeline (4) is arranged on the second liquid discharge port (5), and a second liquid discharge valve (8) is further arranged on the second liquid discharge pipeline (4).
6. The separation and recovery device for aromatic hydrocarbons in hydrogen peroxide oxidized tail gas according to claim 1, characterized in that: the lower part of the separation tank (12) is provided with a through hole matched with the draft tube (2).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201920942406.XU CN210356338U (en) | 2019-06-21 | 2019-06-21 | Hydrogen peroxide solution oxidation tail gas aromatic separation recovery unit |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201920942406.XU CN210356338U (en) | 2019-06-21 | 2019-06-21 | Hydrogen peroxide solution oxidation tail gas aromatic separation recovery unit |
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| Publication Number | Publication Date |
|---|---|
| CN210356338U true CN210356338U (en) | 2020-04-21 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201920942406.XU Active CN210356338U (en) | 2019-06-21 | 2019-06-21 | Hydrogen peroxide solution oxidation tail gas aromatic separation recovery unit |
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| Country | Link |
|---|---|
| CN (1) | CN210356338U (en) |
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2019
- 2019-06-21 CN CN201920942406.XU patent/CN210356338U/en active Active
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