CN215138346U - Hydrogen recovery and non-methane total hydrocarbon deep purification device of chlorine-ethylene-containing mixed gas - Google Patents
Hydrogen recovery and non-methane total hydrocarbon deep purification device of chlorine-ethylene-containing mixed gas Download PDFInfo
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- CN215138346U CN215138346U CN202121108175.6U CN202121108175U CN215138346U CN 215138346 U CN215138346 U CN 215138346U CN 202121108175 U CN202121108175 U CN 202121108175U CN 215138346 U CN215138346 U CN 215138346U
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Abstract
The utility model belongs to the technical field of chemical gas treatment equipment, specifically be hydrogen recovery and non-methane total hydrocarbon deep purification device of chlorine ethylene gas mixture. The device comprises a raw material gas buffer tank, a recovery tower, a vacuum pump unit, a desorption gas buffer tank I, a desorption gas buffer tank II, a heat exchanger, a heater, a purification tower, a supercharger I and a supercharger II, wherein raw material gas is sequentially connected with the raw material gas buffer tank and the recovery tower through the supercharger I; the recovery tower is connected with the desorption gas buffer tank I, the recovery tower is connected with the desorption gas buffer tank II through the vacuum pump unit, and the booster II, the heater, the purification tower, the heat exchanger and the like are sequentially arranged behind the desorption gas buffer tank II. The utility model discloses simple process, degree of automation are high, the small investment, running cost are low, safe environmental protection and energy saving, but wide application in chlor-alkali and PVC production industry.
Description
Technical Field
The utility model belongs to the technical field of chemical gas treatment equipment, specifically be hydrogen recovery and non-methane total hydrocarbon deep purification device of chlorine ethylene gas mixture.
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 of respectively separating and recovering vinyl chloride, acetylene and hydrogen in tail gas by adopting a pressure swing adsorption separation technology and a pressure swing adsorption separation device, wherein 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 vinyl chloride and the acetylene, the exhaust gas of the process flows is the purified gas of the device and mainly contains hydrogen, nitrogen and trace non-methane total hydrocarbon, the purified gas is directly discharged, and the discharge pressure is usually more than 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, and the desorbed gas of the process flow is the exhaust gas and mainly contains a large amount of nitrogen, a small amount of hydrogen and trace non-methane total hydrocarbons.
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 use of low-mercury catalysts, the contents of vinyl chloride and acetylene in the rectification off-gas deviate more than the initial design values. In addition, some enterprises expand production and reform, the amount of the rectification tail gas is greatly increased, the load of the original adsorption separation device is increased by the increase of the content and the flow, 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, in addition, part of non-methane total hydrocarbons can not be consumed in the system cycle production process, and the content of the non-methane total hydrocarbons is increased due to long-time accumulation, so that the emission index of some adsorption separation devices can not reach the original design index and emission standard; therefore, the exhaust gas of the original adsorption separation device needs further advanced purification treatment. The further advanced treatment of the exhaust gas presents the following difficulties:
1. the non-methane total hydrocarbon content is low, the adsorption effect of the conventional adsorbent is poor, and the treated adsorbent cannot reach the new national emission standard.
2. Part of non-methane total hydrocarbons cannot be consumed in the system circulation production, and the content of the non-methane total hydrocarbons in the exhaust gas exceeds the standard after long-time accumulation.
3. The hydrogen content in the exhaust gas is high, so that the catalytic reaction heat is more, and certain potential safety hazard is caused.
4. Some exhaust gases have low pressure and large fluctuation and are not easy to recycle.
5. After the exhaust gas is treated by conventional pressure swing adsorption, the content of non-methane total hydrocarbons can be concentrated, and the content is easier to exceed the national emission standard.
Therefore, it is urgently needed to design and develop a hydrogen recovery and non-methane total hydrocarbon deep purification device for a chlorine-ethylene-containing mixed gas with high purification degree, so as to reduce the damage of chemical enterprises to the environment and recover hydrogen with economic value.
Disclosure of Invention
The invention aims to solve the technical problems and provide the hydrogen recovery and non-methane total hydrocarbon deep purification device containing the vinyl chloride mixed gas, which has the advantages of simple process, low operation cost, high automation degree, small occupied area, less investment and convenient installation.
In order to achieve the above purpose, the specific technical solution of the present invention is:
the device comprises a raw material gas buffer tank, a recovery tower, a vacuum pump unit, a desorption gas buffer tank I, a desorption gas buffer tank II, a heat exchanger, a heater, a purification tower, a supercharger I and a supercharger II, wherein the raw material gas is sequentially connected with the raw material gas buffer tank and the recovery tower through the supercharger I; the recovery tower is connected with desorption gas buffer tank I, and the recovery tower passes through the vacuum pump unit and is connected with desorption gas buffer tank II, sets gradually booster compressor II, heater, purifying column and heat exchanger behind desorption gas buffer tank II, all establishes ties through the pipeline between desorption gas buffer tank II, booster compressor II, heater, purifying column and the heat exchanger.
As a preferred embodiment in the present application, the recovery tower comprises a raw material gas inlet, a final flushing inlet, a purified gas outlet, a flushing inlet, an air pumping outlet and a reverse air discharging outlet; wherein, the raw material gas inlet, the reverse-bleeding gas outlet and the air extraction outlet of the recovery tower are all arranged at the bottom end of the recovery tower; the final flushing inlet, the purified gas outlet and the flushing inlet are all arranged at the top end of the recovery tower.
As a preferred embodiment in the present application, the raw material gas buffer tank is connected to the raw material gas inlet of the recovery tower, the final flushing inlet is connected to the purified gas outlet of the recovery tower through a pipeline, and the flushing inlet is connected to the purified gas outlet of the recovery tower through a pipeline; the air pumping outlet is connected with the vacuum pump unit through a pipeline, and the reverse-release air outlet is connected with the desorption air buffer tank I through a pipeline; the air inlet is connected with the desorption gas buffer tank II through a pipeline.
As a better implementation mode in the application, the recovery tower is provided with the program control valves which are connected with the control device.
In a preferred embodiment of the present invention, the number of the recovery towers is 3 to 10, and the recovery towers are connected in parallel. The recovery tower is filled with a composite adsorbent filler consisting of alumina, activated carbon, silica gel and a molecular sieve, and the adsorbent realizes the adsorption of gases such as non-methane total hydrocarbon.
As a better implementation mode in this application, desorption gas buffer tank I and desorption gas buffer tank II between be equipped with the governing valve.
As a better implementation mode in the application, a regulating valve is arranged between the purified gas outlet and the flushing inlet of the recovery tower.
As a better implementation mode in the application, a regulating valve is arranged between the purified gas outlet and the final flushing inlet of the recovery tower.
As a better embodiment in the application, a regulating valve is arranged between the air inlet and the desorption gas buffer tank II.
In a preferred embodiment of the present invention, the supercharger i is provided with a bypass. By designing a supercharger and a bypass, aiming at the working condition of low pressure of raw material gas, the raw material gas is supercharged by the supercharger and then is introduced into a recovery tower; aiming at the working condition of higher pressure of the raw gas, the raw gas can be directly introduced into the recovery tower through the booster bypass.
The working principle of the device is as follows:
the method comprises the following steps that vinyl chloride vent gas enters a deep purification and hydrogen extraction device under the pressure of about 0.01-0.5 MPa, raw material gas firstly passes through a supercharger or a supercharger bypass and then automatically enters a regenerated recovery tower through a preset program control system, the raw material gas is separated through an adsorbent filled in the recovery tower, impurities such as nitrogen and non-methane total hydrocarbon are adsorbed by the adsorbent and stay in the tower, and hydrogen with the byproduct content of more than or equal to 99.9% is discharged from the top of the tower. After adsorption of one recovery tower is finished, a part of residual gas in the tower is placed into the other recovery tower from the top of the tower, then the other part of residual gas is placed into a desorption gas buffer tank from the bottom of the tower, nitrogen, non-methane total hydrocarbons and the like which are adsorbed and remained in the adsorbent are desorbed by adopting a vacuumizing and vacuumizing flushing mode, regeneration of the adsorbent is realized, simultaneously desorption gas containing the non-methane total hydrocarbons and a certain amount of air are mixed and pressurized and then enter a purification tower for catalytic reaction, and finally the desorption gas after the non-methane total hydrocarbons are removed reaches the national emission standard and is directly discharged. After the regeneration of one recovery tower is finished, the pressure of the recovery tower is raised to the adsorption pressure by utilizing partial purified gas, and the recovery tower is prepared to enter the next adsorption process. The whole process is circularly operated by at least 3 recovery 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 device leads the vinyl chloride-containing vent gas to the bottom of a recovery tower filled with an adsorbent, the adsorbent adsorbs impurities such as nitrogen, non-methane total hydrocarbons and the like, hydrogen with the content of more than or equal to 99.9 percent is discharged from the top of the tower, the impurities adsorbed by the adsorbent are desorbed in a reverse discharge and evacuation mode and further desorbed by a purification tower to remove the non-methane total hydrocarbons, so that the content of the non-methane total hydrocarbons in the desorbed gas is lower than the latest national emission standard, even can meet the stricter requirements of partial regions, and the content of the non-methane total hydrocarbons in the vent gas is less than or equal to 20mg/m3。
The purified gas outlet of the recovery tower is provided with a regulating valve to stabilize the pressure of the device. The device is contrary gassing and air pumping can carry desorption gas buffer tank (I II) earlier, be equipped with governing valve regulated pressure on desorption gas buffer tank I and the pipeline of desorption gas buffer tank II. The air inlet of the device is provided with a regulating valve for controlling the air inflow.
The purge step is terminated and the purge gas is evacuated to reflux a portion of the purge gas.
Compared with the prior art, the utility model discloses an actively the effect is embodied at:
through the design of the raw material gas buffer tank, the raw material gas can enter the recovery tower more stably and continuously.
The device adopts a pressure swing adsorption mode to remove the non-methane total hydrocarbon, which not only produces hydrogen with the content more than or equal to 99.9 percent, but also can ensure that the content of the non-methane total hydrocarbon in the vent gas reaches the latest national emission standard, even can meet the stricter requirements of partial areas, and ensure that the content of the non-methane total hydrocarbon in the vent gas is less than or equal to 20mg/m3。
Thirdly, by designing a supercharger and a bypass, aiming at the working condition of low pressure of the raw material gas, the raw material gas is supercharged by the supercharger and then is introduced into the recovery tower; aiming at the working condition of higher pressure of the raw gas, the raw gas can be directly introduced into the recovery tower through the booster bypass.
And (IV) most of product hydrogen is firstly separated by the device, so that the hydrogen content of desorbed gas in the catalysis step is reduced, the heat release in the catalysis step is reduced, and the safety of the catalysis step is ensured.
Drawings
FIG. 1 is a schematic diagram showing the connection relationship between the non-methane total hydrocarbon deep purification and hydrogen extraction device of the vinyl chloride vent gas of the present invention.
Wherein, 1 is a raw material gas buffer tank; 2-recovery column; 3-vacuum pump; 4-desorption gas buffer tank I; 5-desorption gas buffer tank II; 6-heater; 7-a purification column; 8-supercharger I; 9-supercharger II; 10-recovery tower final flushing inlet; 11-the purified gas outlet of the recovery tower; 12-recovery column purge gas inlet; 13-recovery tower extraction air outlet; 14-reverse vent gas outlet of the recovery tower; 15-raw material gas outlet of the recovery tower; 16-air inlet; 17-program control valve, 18-regulating valve and 19-heat exchanger.
Detailed Description
Hydrogen recovery and non-methane total hydrocarbon deep purification device of chlorine ethylene mist, the device is including retrieving the tower, raw materials gas buffer tank, desorption gas buffer tank (I/II), the vacuum pump, booster compressor I, booster compressor II, the heat exchanger, the heater, the purifying column, the program controlled valve, the governing valve all sets up the program controlled valve on the every pipeline, the raw materials gas passes through the booster compressor, raw materials gas buffer tank, the raw materials gas import, pipeline and program controlled valve are connected with retrieving the tower, retrieve tower and desorption gas buffer tank (I/II) and all with vacuum pump connection, desorption gas buffer tank (I/II) pass through pipeline and booster compressor II, the heater, purifying column and heat exchanger are connected. The reverse air discharge and air pumping of the device are mixed with air and then conveyed to a desorption air buffer tank II.
The recovery tower comprises a raw material gas inlet of the recovery tower, a purified gas outlet of the recovery tower, a final flushing gas inlet, a flushing gas inlet, an air pumping outlet and a reverse-bleeding gas outlet; the washing gas import is through governing valve and recovery tower purification gas exit linkage, and the export of drawing air passes through pipeline and vacuum pump connection, and the export of contrary gassing is connected with desorption gas buffer tank I through the pipeline, and desorption gas buffer tank I passes through the governing valve with desorption gas buffer tank II and is connected, and air intlet is connected through the governing valve with desorption gas buffer tank II.
The number of the recovery towers is 3-10, preferably 5, and all the recovery towers are connected in parallel. And the recovery tower is provided with program control valves which are connected with a control device. The recovery tower is filled with a composite adsorbent filler which is one or more of activated carbon, silica gel, alumina and molecular sieve. Wherein the molecular sieve is modified, the adsorption effect of gases such as non-methane total hydrocarbon is good, and the desorption is relatively easy. The catalyst can safely and effectively remove non-methane total hydrocarbons.
The following description of the embodiments of the present invention is provided for illustrative purposes, and other advantages and effects of the present invention will be readily apparent to those skilled in the art from the disclosure herein. The present invention can also be implemented or applied through other different specific embodiments, and various details in the present specification can be modified or changed based on different viewpoints and applications without departing from the spirit of the present invention. It is to be noted that the features in the following embodiments and examples may be combined with each other without conflict.
It should be noted that, in order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention are clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are some embodiments of the present invention, not all embodiments. The components of embodiments of the present invention, as generally described and illustrated in the figures herein, may be arranged and designed in a wide variety of different configurations.
Thus, the following detailed description of the embodiments of the present invention, presented in the accompanying drawings, is not intended to limit the scope of the invention, as claimed, but is merely representative of selected embodiments of the invention. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative efforts belong to the protection scope of the present invention.
It should be noted that: like reference numbers and letters refer to like items in the following figures, and thus, once an item is defined in one figure, it need not be further defined and explained in subsequent figures.
In the description of the present invention, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", and the like indicate the position or positional relationship based on the position or positional relationship shown in the drawings, or the position or positional relationship which is usually placed when the product of the present invention is used, and are only for convenience of description and simplification of the description, but do not indicate or imply that the device or element referred to must have a specific position, be constructed and operated in a specific orientation, and thus, should not be construed as limiting the present invention. Furthermore, the terms "first," "second," "third," and the like are used solely to distinguish one from another and are not to be construed as indicating or implying relative importance.
Furthermore, the terms "horizontal", "vertical", "overhang" and the like do not imply that the components are required to be absolutely horizontal or overhang, but may be slightly inclined. For example, "horizontal" merely means that the direction is more horizontal than "vertical" and does not mean that the structure must be perfectly horizontal, but may be slightly inclined.
In the description of the present invention, it should also be noted that, unless otherwise explicitly specified or limited, the terms "disposed," "mounted," "connected," and "connected" are to be construed broadly, e.g., as meaning either a fixed connection, a removable connection, or an integral connection; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meaning of the above terms in the present invention can be understood in specific cases to those skilled in the art.
Additionally, the utility model discloses it is pointed out that, in the utility model, if do not write out structure, connection relation, positional relationship, power source relation etc. that concretely relates to very much, then the utility model relates to a structure, connection relation, positional relationship, power source relation etc. are technical personnel in the field on prior art's basis, can not learn through creative work.
Example 1:
as shown in fig. 1, the device for recovering hydrogen containing vinyl chloride mixed gas and deeply purifying non-methane total hydrocarbon comprises a raw material gas buffer tank, a recovery tower, a vacuum pump unit, a desorption gas buffer tank I, a desorption gas buffer tank II, a heat exchanger, a heater, a purification tower, a supercharger I and a supercharger II, wherein the raw material gas is sequentially connected with the raw material gas buffer tank and the recovery tower through the supercharger I; the recovery tower is connected with desorption gas buffer tank I, and the recovery tower passes through the vacuum pump unit and is connected with desorption gas buffer tank II, sets gradually booster compressor II, purifying column, heater and heat exchanger behind desorption gas buffer tank II (booster compressor II, purifying column, heater and heat exchanger all establish ties through the pipeline).
Each pipeline is provided with a program control valve, feed gas containing micro chloroethylene, acetylene and other non-methane total hydrocarbons is connected with a recovery tower through a feed gas buffer tank, a feed gas inlet pipeline and the program control valve, the recovery tower and a desorption gas buffer tank (I/II) are connected with a vacuum pump, and the desorption gas buffer tank (I/II) is connected with a heat exchanger through a supercharger II, a heater and a purification tower. The reverse air discharge and air suction of the device are firstly transmitted to a desorption air buffer tank (I/II).
The recovery tower comprises a raw material gas inlet of the recovery tower, a purified gas outlet of the recovery tower, a flushing gas inlet, a final flushing gas inlet, an air pumping outlet and a reverse-bleeding gas outlet; the washing gas import is through governing valve and recovery tower purification gas exit linkage, and the import of dashing at end is through governing valve and recovery tower purification gas exit linkage, and the pump-out export passes through pipeline and vacuum pump connection, and the export of going back the gassing is passed through the pipeline and is connected with desorption gas buffer tank I, and desorption gas buffer tank I passes through the governing valve with desorption gas buffer tank II and is connected, and air intlet passes through the governing valve and is connected with desorption gas buffer tank II.
The number of the recovery towers is 5, and the recovery towers are connected in parallel. And the recovery tower is provided with program control valves which are connected with a control device. The recovery tower is filled with one or more of composite adsorbent fillers of activated carbon, silica gel, alumina and molecular sieve, and the purification tower is filled with a special catalyst.
The pressure of the discharged gas of the pressure swing adsorption of the rectification tail gas is 0.5MPa, and the gas quantity is about 800Nm3The composition,/h, is shown in the following table:
TABLE 1 composition of hydrogen production and vent gas (V%)
When the adsorption separation device operates, raw gas containing trace chloroethylene, acetylene and other non-methane total hydrocarbons firstly passes through a bypass of a supercharger I, then automatically enters into the regenerated recovery tower through a preset program control system, and is separated by an adsorbent filled in the recovery tower, and hydrogen with the byproduct content of more than or equal to 99.9 percent is discharged from the top of the tower. After adsorption of one recovery tower is finished, a part of residual gas in the tower is placed into the other recovery tower from the top of the tower, then the other part of residual gas is placed into a desorption gas buffer pipe from the bottom of the tower, and finally, the non-methane total hydrocarbon adsorbed and remained in the adsorbent is desorbed by adopting a vacuumizing and flushing mode to realize regeneration of the adsorbent. After the regeneration of one recovery tower is finished, the pressure of the recovery tower is raised to the adsorption pressure by utilizing partial purified gas, and the recovery tower is prepared to enter the next adsorption process. The whole process is circularly operated by at least 3 recovery 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 is processed, the content of the byproduct hydrogen is more than or equal to 99.9 percent, and the exhaust gas reaches the new national emission standard.
Example 2:
as shown in fig. 1, the device for recovering hydrogen containing vinyl chloride mixed gas and deeply purifying non-methane total hydrocarbon comprises a raw material gas buffer tank, a recovery tower, a vacuum pump unit, a desorption gas buffer tank I, a desorption gas buffer tank II, a heat exchanger, a heater, a purification tower, a supercharger I and a supercharger II, wherein the raw material gas is sequentially connected with the raw material gas buffer tank and the recovery tower through the supercharger I; the recovery tower is connected with the desorption gas buffer tank I, the recovery tower is connected with the desorption gas buffer tank II through the vacuum pump unit, and the booster II, the heater, the purification tower and the heat exchanger are sequentially arranged behind the desorption gas buffer tank II. All set up the program control valve on every pipeline, the feed gas passes through the raw materials gas buffer tank, the feed gas inlet pipeline and the program control valve is connected with the recovery tower, and recovery tower and desorption gas buffer tank (I II) all are connected with the vacuum pump, and desorption gas buffer tank (I II) is connected with the heat exchanger through booster compressor II, heater and purifying column. The reverse air discharge and air suction of the device are firstly transmitted to a desorption air buffer tank (I/II).
The recovery tower comprises a raw material gas inlet of the recovery tower, a purified gas outlet of the recovery tower, a flushing gas inlet, a final flushing gas inlet, an air pumping outlet and a reverse-bleeding gas outlet; the washing gas import is through governing valve and recovery tower purification gas exit linkage, and the import of dashing at end is through governing valve and recovery tower purification gas exit linkage, and the pump-out export passes through pipeline and vacuum pump connection, and the export of going back the gassing is passed through the pipeline and is connected with desorption gas buffer tank I, and desorption gas buffer tank I passes through the governing valve with desorption gas buffer tank II and is connected, and air intlet passes through the governing valve and is connected with desorption gas buffer tank II.
The number of the recovery towers is 5, and the recovery towers are connected in parallel. And the recovery tower is provided with program control valves which are connected with a control device. The recovery tower is filled with one or more of composite adsorbent fillers of activated carbon, silica gel, alumina and molecular sieve, and the purification tower is filled with a special catalyst.
The pressure of the rectification tail gas pressure swing adsorption vent gas is 0.01MPa, and the gas quantity is about 100Nm3The composition,/h, is shown in the following table:
TABLE 2 composition of hydrogen production and vent gas (V%)
When the adsorption separation device operates, raw gas containing trace chloroethylene, acetylene and other non-methane total hydrocarbons is firstly pressurized to 0.3MPa by a supercharger I, then automatically enters a regenerated recovery tower through a preset program control system, is separated by an adsorbent filled in the recovery tower, and hydrogen with the byproduct content of more than or equal to 99.9 percent is discharged from the top of the tower. After adsorption of one recovery tower is finished, a part of residual gas in the tower is placed into the other recovery tower from the top of the tower, then the other part of residual gas is placed into a desorption gas buffer pipe from the bottom of the tower, and finally, the non-methane total hydrocarbon adsorbed and remained in the adsorbent is desorbed by adopting a vacuumizing and flushing mode to realize regeneration of the adsorbent. After the regeneration of one recovery tower is finished, the pressure of the recovery tower is raised to the adsorption pressure by utilizing partial purified gas, and the recovery tower is prepared to enter the next adsorption process. The whole process is circularly operated by at least 3 recovery 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 is processed, the content of the byproduct hydrogen is more than or equal to 99.9 percent, and the exhaust gas reaches the new national emission standard.
The foregoing basic embodiments and various further alternative embodiments of the present invention can be freely combined to form multiple embodiments, all of which are embodiments of the present invention that can be adapted and claimed. In the scheme of the utility model, each selection example can be combined with any other basic examples and selection examples at will. Numerous combinations will be known to those skilled in the art.
The above description is only exemplary of the present invention and should not be taken as limiting the scope of the present invention, as any modifications, equivalents, improvements and the like made within the spirit and principles of the present invention are intended to be included within the scope of the present invention.
Claims (10)
1. Hydrogen recovery and non-methane total hydrocarbon deep purification device of chlorine ethylene mist, the device include raw materials gas buffer tank (1), recovery tower (2), vacuum pump unit (3), desorption gas buffer tank I (4), desorption gas buffer tank II (5), heater (6), purifying column (7), booster compressor I (8), booster compressor II (9), heat exchanger (19), its characterized in that: the raw material gas is sequentially connected with a raw material gas buffer tank (1) and a recovery tower (2) through a supercharger I (8); the recovery tower (2) is connected with the desorption gas buffer tank I (4), the recovery tower (2) is connected with the desorption gas buffer tank II (5) through a vacuum pump unit (3), and a booster II (9), a heater (6), a purification tower (7) and a heat exchanger (19) are sequentially arranged behind the desorption gas buffer tank II (5).
2. The apparatus for hydrogen recovery and deep purification of non-methane total hydrocarbons according to claim 1, wherein: the recovery tower (2) comprises a recovery tower raw material gas inlet (15), a final flushing inlet (10), a purified gas outlet (11), a flushing inlet (12), an air extraction outlet (13) and a reverse air discharge outlet (14); wherein, the raw gas inlet (15), the reverse-bleeding gas outlet (14) and the air extraction outlet (13) of the recovery tower are all arranged at the bottom end of the recovery tower (2); the final flushing inlet (10), the purified gas outlet (11) and the flushing inlet (12) are all arranged at the top end of the recovery tower (2).
3. The apparatus for hydrogen recovery and deep purification of non-methane total hydrocarbons according to claim 2, wherein: the raw material gas buffer tank (1) is connected with a raw material gas inlet (15) of the recovery tower, the final flushing inlet (10) is connected with a purified gas outlet (11) of the recovery tower through a pipeline, and the flushing inlet (12) is connected with a purified gas outlet (11) of the recovery tower through a pipeline; the air pumping outlet (13) is connected with the vacuum pump unit (3) through a pipeline, and the reverse air discharging outlet (14) is connected with the desorption air buffer tank I (4) through a pipeline; the air inlet (16) is connected with the desorption gas buffer tank II (5) through a pipeline.
4. The apparatus for hydrogen recovery and deep purification of non-methane total hydrocarbons according to claim 1, wherein: the recovery tower (2) is provided with a program control valve (17), and the program control valve (17) is connected with a control device.
5. The apparatus for hydrogen recovery and deep purification of non-methane total hydrocarbons according to claim 1, wherein: the number of the recovery towers (2) is 3-10, and all the recovery towers are connected in parallel.
6. The apparatus for recovering hydrogen from a vinyl chloride-containing gas mixture and deeply purifying non-methane total hydrocarbons according to claim 3, wherein: and a regulating valve is arranged between the desorption gas buffer tank I (4) and the desorption gas buffer tank II (5).
7. The apparatus for recovering hydrogen from a vinyl chloride-containing gas mixture and deeply purifying non-methane total hydrocarbons according to claim 3, wherein: and a regulating valve is arranged between the purified gas outlet (11) and the flushing inlet (12) of the recovery tower.
8. The apparatus for recovering hydrogen from a vinyl chloride-containing gas mixture and deeply purifying non-methane total hydrocarbons according to claim 3, wherein: and a regulating valve is arranged between the purified gas outlet (11) and the final flushing inlet (10) of the recovery tower.
9. The apparatus for recovering hydrogen from a vinyl chloride-containing gas mixture and deeply purifying non-methane total hydrocarbons according to claim 3, wherein: and an adjusting valve is arranged between the air inlet (16) and the desorption gas buffer tank II (5).
10. The apparatus for hydrogen recovery and deep purification of non-methane total hydrocarbons according to claim 1, wherein: the supercharger I (8) is provided with a bypass.
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| CN202121108175.6U CN215138346U (en) | 2021-05-21 | 2021-05-21 | Hydrogen recovery and non-methane total hydrocarbon deep purification device of chlorine-ethylene-containing mixed gas |
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| CN202121108175.6U CN215138346U (en) | 2021-05-21 | 2021-05-21 | Hydrogen recovery and non-methane total hydrocarbon deep purification device of chlorine-ethylene-containing mixed gas |
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