CN211635878U - Deep purification device for gas containing chloroethylene, acetylene and non-methane total hydrocarbon - Google Patents
Deep purification device for gas containing chloroethylene, acetylene and non-methane total hydrocarbon Download PDFInfo
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Abstract
The utility model belongs to the technical field of chemical gas treatment equipment, specifically be the gaseous deep purification device of the total hydrocarbon of chloroethylene, acetylene and non-methane. The device is an adsorption separation device and comprises a purification tower, a raw material gas buffer tank, a desorption gas buffer tank, a cooler, a program control valve and an automatic control system, wherein all structural steps in the device sequentially undergo adsorption, pressure equalization, reverse pressure relief, evacuation flushing, pressure equalization rising and final pressure rising in a circulating mode. The device adsorbs the components such as chloroethylene, acetylene and non-methane total hydrocarbon in the adsorption step, so that the contents of the chloroethylene, the acetylene and the non-methane total hydrocarbon in the discharged purified gas are respectively less than or equal to 10mg/m3And 50mg/m3The product reaches the latest national emission standard and can be directly discharged after purification treatment; and simultaneously, the chloroethylene, the acetylene and the non-methane total hydrocarbon are desorbed and recovered in the steps of reverse pressure release and evacuation, and the recovery rate of the chloroethylene, the acetylene and the non-methane total hydrocarbon reaches more than 99 percent. The utility model discloses the small investment, running cost are low.
Description
Technical Field
The utility model belongs to the technical field of chemical gas treatment equipment, specifically be the deep purification device who contains gases such as vinyl chloride, acetylene and non-methane total hydrocarbon.
Background
Vinyl chloride is an important chemical raw material, and PVC produced by vinyl chloride polymerization is the most common plastic in the world. The product can be widely applied to building materials, industrial products, daily necessities, floor leathers, floor tiles, artificial leather, pipes, wires and cables, packaging films, bottles, foaming materials, sealing materials, fibers and the like.
During the production of PVC, the rectification system discharges a large amount of tail gas containing components such as vinyl chloride, acetylene, hydrogen, nitrogen and other non-methane total hydrocarbons. The method mainly comprises the following steps that (1) a pressure swing adsorption separation technology and a pressure swing adsorption separation device are generally adopted to respectively separate and recover chloroethylene, acetylene and hydrogen in tail gas, at present, two process flows are mainly adopted, which can be called as a first-stage process and a second-stage process for short, wherein the first-stage process mainly recovers the chloroethylene and the acetylene, the exhaust gas of the process flows is the purified gas of the device and mainly contains hydrogen, nitrogen and trace chloroethylene and acetylene, and for enterprises capable of realizing chlorine balance, the hydrogen does not need to be further recovered, the purified gas is directly discharged, and the discharge pressure is generally above 0.3 MPa; the other process flow is to add a hydrogen extraction device in series on the basis of a one-stage method, further recover hydrogen from the purified gas of the one-stage device, the desorbed gas of the process flow is exhaust gas which mainly contains a large amount of nitrogen, a small amount of hydrogen, trace vinyl chloride, acetylene and other non-methane total hydrocarbons, and the pressure of the exhaust gas is usually normal pressure. The early adsorption separation recovery device is designed mainly according to the integrated emission standard of atmospheric pollutants (GB 16297-3And 120mg/m3。
The adsorption separation device has good effect at the initial stage of operation, and the emission index meets the requirements of design and environmental protection. However, in recent years, with the widespread application of low-mercury catalysts, the contents of vinyl chloride and acetylene in the rectification tail gas deviate more than the initial design value, and particularly the acetylene content is even multiplied. In addition, some enterprises expand production and reform, the amount of the rectification tail gas is greatly increased, the load of the original adsorption and separation device is increased by the increase of the content and the flow, and meanwhile, the adsorption performance of the adsorbent of the original device is gradually reduced along with the increase of the operation time of the pressure swing adsorption device, so that the emission index of some adsorption and separation devices cannot reach the original design index and emission standard; the emission requirement of new emission standard of caustic soda and polyvinyl chloride industrial pollutants (GB15581-2016) promulgated in 2016 cannot be met, and the standard stipulates that the content of vinyl chloride in the exhaust gas is less than or equal to 10mg/m3The content of non-methane total hydrocarbon is less than or equal to 50mg/m3Even in the parts with fragile atmosphere and ecological environment, the required vinyl chloride content is less than or equal to 1mg/m3The content of non-methane total hydrocarbon is less than or equal to 20mg/m3. Therefore, the exhaust gas of the original adsorption separation device still needs further advanced purification treatment. But the exhaust gas has the characteristics of low pressure, large fluctuation, intermittence and the like, which brings difficulty to further deep purification treatment. The further advanced treatment of the exhaust gas presents the following difficulties:
1. the exhaust gas is desorption gas of the adsorption separation device, is pumped out by a vacuum pump unit, and has low pressure which is generally not more than 10KPa and even possibly less than 1 KPa.
2. The gas is pumped out through a vacuum pump unit, the characteristic of intermittent gas transmission exists, the instantaneous flow fluctuation is large, the flow rate reaches hundreds of square meters per hour at the initial stage, and only tens of square meters per hour are possibly generated at the later stage.
3. The content of chloroethylene, acetylene and non-methane total hydrocarbon is low, the pressure of exhaust gas is low, the partial pressure of chloroethylene and acetylene is lower, the adsorption effect of the conventional adsorbent is very poor, and the treated adsorbent cannot reach the new national emission standard.
4. The exhaust gas is an evacuated desorption gas, is a process gas enriched mixed gas of a front device, possibly contains moisture and is concentrated, and the requirement on an adsorbent of a downstream purification treatment device is higher.
5. In the process of evacuation and desorption, air can be sucked in, so that the oxygen content is increased, and potential safety hazards exist.
Therefore, it is urgently needed to design and develop a chloroethylene tail gas vent gas deep purification device with high purification degree and safety so as to reduce the damage of chemical enterprises to the environment.
Disclosure of Invention
The present invention is directed to solve the above problems and to provide a deep purification device for gases containing chloroethylene, acetylene, and non-methane hydrocarbons. The device has the advantages of simple structure, easy operation, low running cost, high automation degree, small occupied area, less investment and convenient installation.
In order to achieve the purpose of the invention, the specific technical scheme of the utility model is as follows:
the deep purification device comprises a raw material gas buffer tank, a compressor unit, a cooler I, a purification tower, a vacuum pump unit, a desorption gas buffer tank I, a desorption gas buffer tank II, a cooler II and a supercharger unit, wherein the raw material gas buffer tank is connected with the cooler I; the cooler I is connected with the compressor unit; the compressor unit is connected with the purification tower through a raw material gas inlet of the purification tower; the purification tower is respectively connected with a vacuum pump unit and a desorption gas buffer tank I, and the vacuum pump unit is connected with a desorption gas buffer tank II; the desorption gas buffer tank I is connected with the desorption gas buffer tank II, and the desorption gas buffer tank II is sequentially connected with the cooler II and the supercharger unit.
The purification tower is provided with a purification tower raw material gas inlet, a purification tower purified gas outlet, a flushing gas inlet, a pressure equalizing gas outlet, an air pumping outlet and a reverse air discharging outlet. The purification tower feed gas inlet, the reverse-bleeding gas outlet and the air pumping outlet are all arranged at the bottom end of the purification tower, and the outlet of the compressor is communicated with the purification tower feed gas inlet through a pipeline; the flushing gas inlet, the purifying gas outlet and the pressure equalizing gas outlet of the purifying tower are all arranged at the top end of the purifying tower; the pressure equalizing gas outlet is connected with a purified gas outlet of the purifying tower through a pipeline; the air pumping outlet is connected with the vacuum pump unit through a pipeline; the reverse-air outlet is connected with the desorption air buffer tank I through a pipeline.
And each outlet of the purification tower is connected with a pipeline, a program control valve is arranged on each pipeline connected with the outlet of the purification tower, and the program control valve is connected with a control device.
The number of the purification towers is 3-10, and the purification towers are connected in parallel. The purifying tower is filled with a composite adsorbent filler consisting of alumina, activated carbon, silica gel and a molecular sieve; can effectively adsorb low-content chloroethylene, acetylene and non-methane total hydrocarbon, and has the advantages of high reuse rate, long service life and thorough regeneration by using lower energy consumption.
And a regulating valve is arranged between the desorption gas buffer tank I and the desorption gas buffer tank II.
And a regulating valve is arranged between the purified gas outlet and the flushing inlet of the purification tower.
The utility model discloses an actively the effect does:
through the design of the raw material gas buffer tank, the raw material gas can enter the purification tower more stably and continuously. The raw material gas compressor is designed to improve the pressure of the raw material gas entering the purification tower and strengthen the adsorption capacity of the adsorbent.
The device adopts pressure swing adsorption to recover chloroethylene and acetylene in the vent gas of the hydrogen production device, thereby ensuring high recovery rate of chloroethylene and acetylene, enabling the contents of chloroethylene and acetylene in the purified gas to reach the latest national emission standard, even meeting the stricter requirements of partial areas, and enabling the content of chloroethylene in the vent gas to be less than or equal to 1mg/m3The content of acetylene and non-methane total hydrocarbon is less than or equal to 20mg/m3。
And (III) because the feed gas is desorbed gas of the front adsorption separation device and is pumped out by the vacuum pump, safety measures such as oxygen content detection can be added as required, and the feed gas is safely interlocked and emptied in the recovery and deep purification processes.
Drawings
FIG. 1 is a schematic structural diagram of an advanced purification apparatus for gases containing chloroethylene, acetylene and non-methane total hydrocarbons according to the present invention;
wherein, 1 is a raw material gas buffer tank; 2, raw material gas inlet of the purification tower; 3-cooler I; 4-compressor; 5-a purification column; 6-vacuum pump unit; 7-desorption gas buffer tank I; 8-desorption gas buffer tank II; 9-cooler II; 10-supercharger; 11-a programmable valve; 12-regulating valve; 13-inlet for flushing gas; 14-purified gas outlet of the purification tower, 15-pressure equalizing gas outlet, 16-air extraction outlet, 17-reverse air outlet.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention will be described in detail with reference to the following embodiments, but it should not be understood that the scope of the above-described subject matter of the present invention is limited to the following embodiments.
The% referred to in this application means the volume percentage, i.e. v%, unless otherwise specified.
Example 1:
as shown in figure 1, the deep purification device for the gases containing chloroethylene, acetylene and non-methane total hydrocarbons comprises a purification tower, a raw material gas buffer tank, a cooler I, a cooler II, a compressor, a supercharger, a program control valve, a desorption gas buffer tank I, a desorption gas buffer tank II, a vacuum pump, a raw material gas inlet of the purification tower and a purified gas outlet of the purification tower, wherein the program control valve is arranged on each pipeline. The feed gas loops through feed gas buffer tank, cooler I, compressor unit, the feed gas import of purifying column bottom, pipeline and programmable valve and is connected with the purifying column, and purifying column, desorption gas buffer tank I and desorption gas buffer tank II all are connected with the vacuum pump, and desorption gas buffer tank I and desorption gas buffer tank II pass through cooler II and are connected with the booster compressor. The reverse air discharge and air suction of the device can be firstly conveyed to a desorption air buffer tank I and a desorption air buffer tank II.
The purification tower is provided with a purification tower raw material gas inlet, a purification tower purified gas outlet, a flushing gas inlet, a pressure equalizing gas outlet, an air pumping outlet and a reverse air discharging outlet. The purification tower feed gas inlet, the reverse-bleeding gas outlet and the air pumping outlet are all arranged at the bottom end of the purification tower, and the outlet of the compressor is communicated with the purification tower feed gas inlet through a pipeline; the flushing gas inlet, the purifying gas outlet and the pressure equalizing gas outlet of the purifying tower are all arranged at the top end of the purifying tower; the pressure equalizing gas outlet is connected with a purified gas outlet of the purifying tower through a pipeline; the air pumping outlet is connected with the vacuum pump unit through a pipeline; the reverse-air outlet is connected with the desorption air buffer tank I through a pipeline.
The flush gas import is through governing valve and purification tower purification gas exit linkage, and the pump air export passes through the pipeline and is connected with vacuum pump, and desorption gas buffer tank I passes through the governing valve with desorption gas buffer tank II and is connected.
The number of the purification towers is 5, and the purification towers are connected in parallel. The purification tower is provided with program control valves which are connected with a control device. The purification tower is filled with one or more composite adsorbent fillers selected from activated carbon, silica gel, alumina and molecular sieves.
The pressure of the hydrogen production vent gas is 1-10 KPa, and the gas amount is about 1000Nm3The hydrogen production vent gas composition is shown in the following table:
TABLE 1 composition of hydrogen production and vent gas (V%)
When the adsorption separation device operates, the raw material gas automatically enters the regenerated purification towers through a preset program control system, and is separated by the adsorbent filled in the purification towers. After the adsorption of one purifying tower is finished, one part of residual gas in the tower is put into a pressure equalizing tank from the top of the tower, then the other part of residual gas is put into a desorption gas buffer pipe from the bottom of the tower, and finally vinyl chloride and acetylene which are adsorbed and remained in the adsorbent are desorbed by adopting a vacuumizing and flushing mode to realize the regeneration of the adsorbent. After the regeneration of one purifying tower is finished, partial purified gas is utilized to boost the pressure of the purifying tower to the adsorption pressure, and the next adsorption process is prepared. The whole process is circularly operated by at least 3 purifying towers, the time is evenly staggered, and the whole switching process is automatically controlled by a preset program system, so that the continuous, stable and safe operation of the device is ensured. The circulation unit process of each tower is as follows: a (adsorption) -ED (pressure drop equalization) -D (reverse discharge) -V/VP (evacuation and evacuation rinse) -ER (pressure rise equalization) -FR (final rise).
After the device in the utility model is processed, the recovery rate of chloroethylene and acetylene in hydrogen production vent gas can reach 99.9 percent, and the purified gas reaches the new national emission standard.
The above description is only a preferred embodiment of the present invention, and should not be taken as limiting the technical solution of the present invention, and any modification, equivalent replacement, and improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (6)
1. The deep purification device who contains vinyl chloride, acetylene and non-methane total hydrocarbon gas, the device include raw materials gas buffer tank (1), compressor unit (4), cooler I (3), purifying column (5), vacuum pump unit (6), desorption gas buffer tank I (7), desorption gas buffer tank II (8), cooler II (9) and booster set (10), its characterized in that: the raw material gas buffer tank (1) is connected with a cooler I (3); the cooler I (3) is connected with the compressor unit (4); the compressor unit (4) is connected with the purification tower (5) through a purification tower raw material gas inlet (2); the purification tower (5) is respectively connected with a vacuum pump unit (6) and a desorption gas buffer tank I (7), and the vacuum pump unit (6) is connected with a desorption gas buffer tank II (8); the desorption gas buffer tank I (7) is connected with the desorption gas buffer tank II (8), and the desorption gas buffer tank II (8) is sequentially connected with the cooler II (9) and the supercharger unit (10).
2. The apparatus for deep purification of a gas containing vinyl chloride, acetylene and non-methane total hydrocarbons according to claim 1, wherein: the purification tower (5) is provided with a purification tower raw material gas inlet (2), a purification tower purified gas outlet (14), a flushing gas inlet (13), a pressure equalizing gas outlet (15), an air extraction outlet (16) and a reverse air discharge outlet (17); wherein the raw material gas inlet (2), the air extraction outlet (16) and the reverse air outlet (17) of the purification tower are all arranged at the bottom end of the purification tower (5); the flushing gas inlet (13), the purifying gas outlet (14) of the purifying tower and the pressure equalizing gas outlet (15) are all arranged at the top end of the purifying tower (5); the pressure equalizing gas outlet (15) is connected with a purified gas outlet (14) of the purification tower through a pipeline, the air pumping outlet (16) is connected with the vacuum pump unit (6) through a pipeline, and the reverse air outlet (17) is connected with the desorption gas buffer tank I (7) through a pipeline.
3. The apparatus for deep purification of a gas containing vinyl chloride, acetylene and non-methane total hydrocarbons according to claim 1, wherein: and the pipelines connected with the purification tower (5) are provided with program control valves (11), and the program control valves (11) are connected with a control device.
4. The apparatus for deep purification of a gas containing vinyl chloride, acetylene and non-methane total hydrocarbons according to claim 1, wherein: the number of the purification towers (5) is 3-10, and the purification towers are connected in parallel.
5. The apparatus for deep purification of a gas containing vinyl chloride, acetylene and non-methane total hydrocarbons according to claim 1, wherein: and a regulating valve is arranged between the desorption gas buffer tank I (7) and the desorption gas buffer tank II (8).
6. The apparatus for deep purification of a gas containing vinyl chloride, acetylene and non-methane total hydrocarbons according to claim 2, wherein: and a regulating valve is arranged between the purified gas outlet (14) and the flushing gas inlet (13) of the purification tower.
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| CN201921469581.8U CN211635878U (en) | 2019-09-05 | 2019-09-05 | Deep purification device for gas containing chloroethylene, acetylene and non-methane total hydrocarbon |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112546810A (en) * | 2020-12-07 | 2021-03-26 | 鄂尔多斯市君正能源化工有限公司 | Efficient hydrogen extraction device for vinyl chloride pressure swing adsorption |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112546810A (en) * | 2020-12-07 | 2021-03-26 | 鄂尔多斯市君正能源化工有限公司 | Efficient hydrogen extraction device for vinyl chloride pressure swing adsorption |
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