CN212417553U - Deep purification system for hydrocarbon compounds - Google Patents
Deep purification system for hydrocarbon compounds Download PDFInfo
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- CN212417553U CN212417553U CN202021506948.1U CN202021506948U CN212417553U CN 212417553 U CN212417553 U CN 212417553U CN 202021506948 U CN202021506948 U CN 202021506948U CN 212417553 U CN212417553 U CN 212417553U
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Abstract
The utility model discloses a deep purification system for hydrocarbon compounds, which comprises a hydrocarbon processing unit, a low-temperature reactor and a high-temperature reactor which are connected in series, and a first heater and a second heater which are arranged in one-to-one correspondence with the low-temperature reactor and the high-temperature reactor, wherein the low-temperature reactor is connected with an air inlet pipeline, the high-temperature reactor is connected with an air outlet pipeline, and the air outlet of the low-temperature reactor is connected with the air inlet of the high-temperature reactor through an intermediate pipeline; the gas to be treated is heated by the first heater, low-temperature catalytic oxidation treatment is completed in the low-temperature reactor, and after heat exchange is performed by the heat exchange module, the gas is heated by the second heater and high-temperature catalytic oxidation treatment is completed in the high-temperature reactor. By adopting the scheme, the high efficiency and stability of pollutant removal and the safety of system reaction are improved, the energy-saving performance and stability of system operation are improved, and the overall manufacturing cost and the processing difficulty of the system are reduced.
Description
Technical Field
The utility model relates to a deep purification system for hydrocarbon compounds, which is used for catalytic oxidation purification treatment of oxygen-containing gas.
Background
Gas such as compressed air is usually required to be purified before being used, and especially, the purification grade of the compressed air is required to be higher in some laboratories or scientific research institutions. The catalytic oxidation is one of the main means for deeply purifying the gas and removing the hydrocarbon pollution in the gas, however, the conventional one-stage catalytic oxidation reaction needs to remove C1～C5The hydrocarbon compound of (2) so that a higher reaction temperature is required, and the high molecular weight C5+The reaction temperature required by the treatment of the hydrocarbon compound is lower, so when pressure-bearing reaction equipment is designed, after the economical efficiency is comprehensively considered, enough margin is not left on the design and selection of equipment materials, and if the hydrocarbon compound in the treated gas fluctuates abnormally, the temperature runaway of a reaction system is easily caused, the pressure-bearing strength of the equipment is reduced rapidly, and the safety accident is caused. In addition, the one-stage reaction mode cannot stably ensure the treatment depth of pollutants, and the quality of product gas is easy to fluctuate.
SUMMERY OF THE UTILITY MODEL
For prior art's not enough more than improving, the utility model provides a deep purification system for hydrocarbon compounds through two segmentation catalytic oxidation, carries out segmentation advanced treatment to the hydrocarbon of different molecular weights to improve equipment operating stability and product quality uniformity etc..
In order to achieve the above purpose, the utility model discloses technical scheme as follows:
a deep purification system for hydrocarbons, comprising a hydrocarbon processing unit, characterized in that: the hydrocarbon processing unit comprises a low-temperature reactor and a high-temperature reactor which are connected in series, and a first heater and a second heater which are arranged in one-to-one correspondence with the low-temperature reactor and the high-temperature reactor, the low-temperature reactor is connected with an air inlet pipeline, the high-temperature reactor is connected with an air outlet pipeline, and an air outlet of the low-temperature reactor is connected with an air inlet of the high-temperature reactor through an intermediate pipeline;
the gas to be treated is heated by the first heater, low-temperature catalytic oxidation treatment is completed in the low-temperature reactor, and after heat exchange is performed through the heat exchange module, the gas is heated by the second heater and high-temperature catalytic oxidation treatment is completed in the high-temperature reactor.
By adopting the structure, the hydrocarbon is separated mainly in a two-section structure, and the front section is separated from the high molecular weight C in a low-temperature reactor under the low-temperature condition5+The latter stage is in high-temperature reactor, under the condition of high temperature removing C1～C5The hydrocarbon compound of (2) can be treated by front-stage treatment and the treatment load in the rear-stage high-temperature reactor is greatly reduced, so that better conditions are created for deeply removing low-molecular hydrocarbon, and the high-molecular-weight C with more content is used5+The hydrocarbon is removed, so that only a small amount of C is available from the atmosphere in the high temperature reactor1～C5The reaction fluctuation of the hydrocarbon compound is small, the reaction sufficiency can be ensured under the action of a high-temperature environment and a catalyst, the system temperature can be effectively controlled under a trace amount of reaction, the temperature runaway phenomenon caused by difficulty in controlling the temperature of a reactor bed layer due to rapid reaction in the high-temperature environment can be effectively avoided, and the safety of the system is greatly improved.
Preferably, the method comprises the following steps: the heat exchange module comprises at least one heat exchanger A and at least one heat exchanger B, the heat exchanger A and the heat exchanger B are sequentially arranged on the intermediate pipeline, and the heat exchanger A is positioned at the upstream of the heat exchanger B;
the heat exchanger A is used for heat exchange between the air inlet pipeline and the middle pipeline, and the heat exchanger B is used for heat exchange between the air outlet pipeline and the middle pipeline. Scheme more than adopting, the temperature of giving vent to anger through the usable low temperature reactor of heat exchanger A preheats its inlet temperature, and the high temperature of giving vent to anger in the usable high temperature reactor of heat exchanger B preheats its inlet temperature, is favorable to make full use of heat energy, reduces the power that corresponds the heater, realizes playing the effect that the unit was given vent to anger and is cooled down simultaneously, avoids causing the damage to high temperature reactor downstream pipeline or equipment.
Preferably, the method comprises the following steps: the heat exchange module comprises at least one heat exchanger A and at least one heat exchanger B, the heat exchanger A and the heat exchanger B are sequentially arranged on an air outlet pipeline of the high-temperature reactor, and the heat exchanger B is positioned at the upstream of the heat exchanger A;
the heat exchanger A is used for heat exchange between the air inlet pipeline and the air outlet pipeline, and the heat exchanger B is used for heat exchange between the middle pipeline and the air outlet pipeline. By adopting the scheme, the heat exchanger A and the heat exchanger B respectively preheat the inlet air of the low-temperature reactor and the outlet air of the high-temperature reactor by utilizing the outlet air high temperature of the high-temperature reactor, the final outlet air temperature of the treatment unit is favorably further reduced, the damage to downstream pipelines and equipment is reduced, the waste heat utilization efficiency is improved, and the like.
Preferably, the method comprises the following steps: the heat exchange module comprises at least one heat exchanger A, at least one heat exchanger B and at least one heat exchanger C, the heat exchanger A, the heat exchanger C and the heat exchanger B are sequentially arranged on the intermediate pipeline, and the heat exchanger A is close to the air outlet of the low-temperature reactor;
the heat exchanger A is used for heat exchange between the air inlet pipeline and the middle pipeline, and the heat exchanger B and the heat exchanger C are both used for heat exchange between the air outlet pipeline and the middle pipeline. By adopting the structure, the air outlet temperature of the low-temperature reactor can be utilized to preheat the air inlet temperature of the low-temperature reactor through the heat exchanger A, the air outlet high temperature of the high-temperature reactor can be utilized to preheat the air inlet temperature of the high-temperature reactor through the heat exchanger B and the heat exchanger C, and on the contrary, the air outlet temperature of the high-temperature reactor is subjected to two-stage cooling through the heat exchanger B and the heat exchanger C, so that the waste heat utilization efficiency is improved, and the air outlet temperature of the unit is further reduced.
Preferably, the method comprises the following steps: the first heater and the second heater are external heaters arranged on pipelines, and/or heating structures arranged inside the reactor, and/or heating structures arranged on the outer wall of the reactor. By adopting the scheme, a proper heater structure can be selected according to the magnitude and the requirement of the treatment gas and from the aspects of economy, environmental places and the like, so that the method has a more universal application range.
Preferably, the method comprises the following steps: the second heater is an external heater arranged on the middle pipeline, the high-temperature reactor is provided with a third heater, and the first heater and the third heater are heating structures extending into the reactor or attached to the outer wall of the reactor. By adopting the scheme, the first heater and the third heater can be operated to preheat the catalyst beds reflected before the system is ventilated in the initial operation stage of the system, and the system starts to operate after the beds reach the set temperature, so that the thermal balance of the system can be quickly established by depending on the heat storage capacity of the beds during preheating after the medium gas to be treated is introduced; in addition, after ventilation is carried out until the heat balance is achieved, the first heater and the third heater still operate so as to provide enough heat for the system, after the heat balance is achieved, the first heater and the third heater can stop operating, heat is provided for the system only by the second heater, and only the system heat loss is compensated, so that the load of the second heater is greatly reduced, the service life of the second heater is prolonged, and the system can rapidly achieve the heat balance.
Preferably, the method comprises the following steps: and temperature sensors are arranged on the low-temperature reactor and the high-temperature reactor. By adopting the structure, the temperature of the catalyst bed layer of the reactor can be monitored and controlled in real time, and carding adjustment is carried out according to the size of equipment, so that the effective monitoring of the system temperature is ensured, and the safety and the stability of the system operation are ensured.
Preferably, the method comprises the following steps: the heat exchange module is detachably arranged on the pipeline and/or integrated on the cylinders of the low-temperature reactor and the high-temperature reactor. By adopting the scheme, the requirements of installation environment or use condition can be met, and when the heat exchanger is integrated on the reactor, the heat loss of gas in the pipeline can be relatively reduced.
To facilitate control of the gas flow into the treatment unit, the inlet and/or outlet lines are provided with shut-off valves.
Compared with the prior art, the beneficial effects of the utility model are that:
adopt the utility model provides a deep purification system for hydrocarbon compounds mainly adopts two segmentation structures to deviate from the processing to the hydrocarbon of different molecular weights in the gas, can effectively avoid because hydrocarbon is undulant at reactor content, the reactor bed temperature that arouses is undulant, reduce the not easily controlled risk of reactor bed temperature that the sharp reaction of high temperature environment caused promptly, improve the whole security of system, utilize heat exchange module to improve the energy-conservation and the stability of system simultaneously, manufacturing cost and the processing degree of difficulty all reduce to some extent.
Drawings
FIG. 1 is a schematic view of a first embodiment of the present invention;
FIG. 2 is a schematic view of a second embodiment of the present invention;
FIG. 3 is a schematic view of a third embodiment of the present invention;
FIG. 4 is a schematic view of a fourth embodiment of the present invention;
fig. 5 is a schematic diagram of a fifth embodiment of the present invention.
Detailed Description
The present invention will be further described with reference to the following examples and accompanying drawings.
Referring to fig. 1 to 4, the deep purification system for hydrocarbons includes a hydrocarbon processing unit, the hydrocarbon processing unit mainly includes a low temperature reactor 1 and a high temperature reactor 2 which are arranged in series, as shown in the figure, an air inlet of the low temperature reactor 1 is connected with an air inlet pipeline 10, an air outlet of the high temperature reactor 2 is connected with an air outlet pipeline 20, an air outlet of the low temperature reactor 1 is communicated with an air inlet of the high temperature reactor 2 through an intermediate pipeline L, in addition, the low temperature reactor 1 and the high temperature reactor 2 are respectively configured with a first heater 3 and a second heater 4, the first heater 3 is mainly used for increasing a gas reaction temperature in the low temperature reactor 1, and the second heater 4 is used for increasing a gas reaction temperature in the high temperature reactor 2.
In addition, be equipped with heat exchange module between low temperature reactor 1 and the high temperature reactor 2, heat exchange module mainly used realizes waste heat and recycles to and low temperature reactor 1 and the effect of high temperature reactor 2 interior reaction gas preheat and reduce the terminal temperature of giving vent to anger of gas outlet pipe way 20.
In the present application, the first heater 3 and the second heater 4 may be external heaters disposed on the pipeline, or may be built-in heating structures extending into the corresponding reactors, such as heating rods, or may be heating structures attached to the outer walls of the corresponding reactors, such as in the form of heating rings, and the first heater 3 and the second heater 4 in the same unit may be a single selection of the above structures, or may be different combinations of the structures, as the case may be.
In addition, the first heater 3 and the second heater 4 may adopt various heating methods such as electric heating, steam heating, heat transfer oil heating, or gas combustion heating.
All be equipped with temperature sensor T on low temperature reactor 1 in this application and the high temperature reactor 2, its mainly used real-time measurement control corresponds the catalyst bed temperature in the reactor to guarantee the effective control to system's temperature, the security and the reliability of side cut system operation.
In order to improve the protection effect on the processing unit, the air inlet pipeline 10 or the air outlet pipeline 20 is provided with the stop valve 8, and the stop valve 8 can be arranged on the air inlet pipeline 10 and the air outlet pipeline 20 at the same time, so that the air flow can be quickly cut off when necessary.
The heat exchange module in the present application may be detachably disposed on different pipes of the unit, or integrally mounted on the cylinder of the low temperature reactor 1 and/or the high temperature reactor 2 to reduce heat loss, or may be a combination of the two methods.
According to the combination mode of the heat exchange module on the pipeline, the application mainly lists the following concentrated embodiments, which are as follows:
in a first embodiment, the heat exchange module includes at least one heat exchanger a5 and at least one heat exchanger B6, which are sequentially disposed on the intermediate pipeline L, wherein the heat exchanger a5 is located upstream of the heat exchanger B6, and the heat exchanger a5 is relatively closer to the gas outlet of the low-temperature reactor 1, wherein the heat exchanger a5 is used for heat exchange between the gas inlet pipeline 10 and the intermediate pipeline L, that is, the gas entering the gas inlet pipeline 10 is preheated by using the outlet heat of the low-temperature reactor 1, and the heat exchanger B6 is used for heat exchange between the gas outlet pipeline 20 and the intermediate pipeline L, and the inlet temperature of the gas is preheated by using the outlet heat of the high-temperature reactor 2.
In this embodiment, the first heater 3 is an internal heating structure extending into the low temperature reactor 1, and the second heater 4 is an external heating structure disposed on the intermediate pipeline L and located between the heat exchanger B6 and the high temperature reactor 6.
In the second and third embodiments, each heat exchange module includes at least one heat exchanger a5 and at least one heat exchanger B6, the heat exchanger a5 and the heat exchanger B6 are sequentially disposed on the gas outlet pipeline 20 of the high temperature reactor 2, and the heat exchanger B6 is located upstream of the heat exchanger a5, that is, the heat exchanger B6 is relatively closer to the gas outlet of the high temperature reactor 2, wherein the heat exchanger a5 is used for heat exchange between the gas inlet pipeline 10 and the gas outlet pipeline 20, and the heat exchanger B6 is used for heat exchange between the intermediate pipeline L and the gas outlet pipeline 20, so that the gas entering the high temperature reactor 2 and the gas entering the low temperature reactor 1 are preheated mainly by using the high temperature of the gas coming out of the high temperature reactor 2, which is beneficial to improving the utilization.
The difference between the second and third embodiments is that the second heater 4 has a different structure, as shown in the figure, the second heater 4 in the second embodiment adopts an external heater and is directly arranged on the intermediate pipeline L and is positioned between the heat exchanger B6 and the high-temperature reactor 2, while the second heater 4 in the third embodiment adopts an internal heating structure, and in addition, the inlet end of the air inlet pipeline 10 and the outlet end of the air outlet pipeline 20 in the third embodiment are both provided with a stop valve 8.
In a fourth embodiment, the heat exchange module includes at least one heat exchanger a5, at least one heat exchanger B6, and at least one heat exchanger C7, the heat exchanger a5, the heat exchanger C7, and the heat exchanger B6 are sequentially disposed on the intermediate pipeline L, wherein the heat exchanger a5 is relatively closer to the gas outlet of the low-temperature reactor 1, the heat exchanger a5 is used for heat exchange between the gas inlet pipeline 10 and the intermediate pipeline L, the inlet gas of the low-temperature reactor 1 is preheated by using the waste heat of the outlet gas, and the heat exchanger B6 and the heat exchanger C7 are both used for heat exchange between the gas outlet pipeline 20 and the intermediate pipeline L, that is, the outlet gas of the high-temperature reactor 2 is preheated by using the outlet gas preheating of the high-temperature reactor 2 through two-stage heat exchange.
In this embodiment, the first heater 3 is a heating structure attached to the outer wall of the low temperature reactor 1, and the second heater 4 is a built-in structure extending into the high temperature reactor 2.
In view of the change of the heating structure of the system, the operation load of the heater, etc., a fifth embodiment is also provided, as shown in the figure, the pipeline connection manner of this embodiment is basically similar to that of the second embodiment, and the second heater 4 is an external heater disposed on the intermediate pipeline L, except that the high-temperature reactor 2 in this embodiment is further provided with a third heater 9, the third heater 9 is a coil heating structure disposed on the outer wall of the high-temperature reactor 2, and may of course be a heating rod extending into the high-temperature reactor, and the first heater 3 is a coil heating structure disposed on the outer wall of the low-temperature reactor 1, in this embodiment, the first heater 3 and the third heater 9 mainly perform a preheating function, and the second heater 4 mainly performs a thermal compensation function.
In the initial stage of system operation, the first heater 3 and the third heater 9 can be operated to preheat the catalyst bed layer in the reactor before the system is ventilated, and the system starts to operate after the bed layer reaches the set temperature, so that the heat balance of the system can be quickly established by depending on the heat storage capacity of the bed layer during preheating after the medium gas to be treated is introduced; in addition, after ventilation and until the thermal balance is achieved, the first heater 3 and the third heater 9 are still operated so as to provide enough heat for the system, after the thermal balance is achieved, the first heater 3 and the third heater 9 can stop operating, and heat is provided for the system only by the second heater 4 so as to compensate the heat loss of the system, so that the load of the second heater 4 is greatly reduced, the service life of the second heater 4 is prolonged, and the system can rapidly achieve the thermal balance.
In the above embodiments, when the heat exchanger a5 and the heat exchanger B6 are both multiple, the multiple heat exchangers a5 are connected in series, and the multiple heat exchangers B6 are also connected in series.
Referring to the deep purification system for hydrocarbons shown in fig. 1 to 4, in use, catalysts are filled in the low-temperature reactor 1 and the high-temperature reactor 2, and the hydrocarbon processing unit is connected into the system through the gas inlet pipeline 10 and the gas outlet pipeline 20, so that the following technical effects are mainly achieved:
firstly, the removal of pollutants is more efficient and stable, the hydrocarbon compounds are removed in two sections, and the high molecular weight C is removed in the front section at low temperature5+The latter stage removes low molecular weight C under high temperature1～C5The hydrocarbon compound is treated by the front-end treatment, so that the treatment load is greatly reduced, and better conditions are created for deeply removing hydrocarbon organic matters. Therefore, the sectional treatment greatly improves the removal efficiency of the system on the hydrocarbon compounds and ensures the stability of the treatment effect.
Secondly, the safety of system reaction is improved, in the two-stage treatment mode, the first-stage low-temperature reactor removes C in a low-temperature oxidation combustion mode5And the above macromolecular hydrocarbons: such substances have a high intrinsic calorific value, which may be carried over during the pressurization of the compression plant, and whose content is relative to C5The following hydrocarbons are much higher and there will be some content fluctuations during system operation due to equipment reasons, causing the temperature of the reactor bed to fluctuate. Therefore, the reaction is removed in a section of low-temperature reactor under a low-temperature condition, the temperature runaway phenomenon caused by the fact that the temperature of a reactor bed layer is not easy to control due to the fact that the reaction is rapidly carried out in a high-temperature environment can be effectively avoided, and the safety of the system is improved.
In the second stage high temperature reactor, due to C5+The material has been completely converted, C1～C5The content of the pollutants is more from the atmosphere and is lower, so that the sufficiency of the reaction can be ensured under the action of a high-temperature environment and a catalyst, and the system temperature can be effectively controlled under the action of trace reaction, so that the system safety is ensured.
And thirdly, the energy-saving performance and the stability of the system operation are improved, the heat exchange modules are additionally arranged in the two sections of reaction systems, the heat in the system can be effectively recycled, the operation of a heater in the system under a low load during the operation period is ensured, and only a small amount of lost heat needs to be supplemented to the system.
In addition, a system structure of two-stage reaction is adopted, so that stepped heating can be effectively realized, and a high-temperature reaction environment can be quickly realized by a rear-stage high-temperature reactor under the condition of lower installed power, so that the energy saving performance of the system can be improved, the system can be ensured to quickly establish thermal balance, and the stable operation of the system can be ensured.
Fourthly, the overall manufacturing cost and the processing difficulty of the system are reduced, two-stage step-by-step reaction is carried out, most of hydrocarbons are treated in a first-stage low-temperature reactor under a low-temperature condition, the treatment capacity is large, but the reaction temperature of equipment is low, so that the requirement on equipment materials is low; the second-stage treatment needs a high-temperature reaction environment, has high requirements on equipment materials, but has low content of low-carbon pollutants and low corresponding reaction load, so that the size of the tower body of the second-stage high-temperature reactor can be greatly reduced, and the processing difficulty and the manufacturing cost of the high-temperature reaction container are reduced.
Finally, it should be noted that the above description is only a preferred embodiment of the present invention, and those skilled in the art can make various similar representations without departing from the spirit and the scope of the present invention.
Claims (9)
1. A deep purification system for hydrocarbons, comprising a hydrocarbon processing unit, characterized in that: the hydrocarbon processing unit comprises a low-temperature reactor (1), a high-temperature reactor (2), a first heater (3) and a second heater (4), wherein the low-temperature reactor (1) and the high-temperature reactor (2) are connected in series, the first heater (3) and the second heater (4) are arranged in one-to-one correspondence to the low-temperature reactor (1) and the high-temperature reactor (2), the low-temperature reactor (1) is connected with an air inlet pipeline (10), the high-temperature reactor (2) is connected with an air outlet pipeline (20), and an air outlet of the low-temperature reactor (1) is connected with an air inlet of the;
the gas to be treated is heated by the first heater (3) and is subjected to low-temperature catalytic oxidation treatment in the low-temperature reactor (1), and after heat exchange by the heat exchange module, the gas is heated by the second heater (4) and is subjected to high-temperature catalytic oxidation treatment in the high-temperature reactor (2).
2. The deep purification system for hydrocarbons according to claim 1, wherein: the heat exchange module comprises at least one heat exchanger A (5) and at least one heat exchanger B (6), the heat exchanger A (5) and the heat exchanger B (6) are sequentially arranged on the middle pipeline (L), and the heat exchanger A (5) is positioned at the upstream of the heat exchanger B (6);
the heat exchanger A (5) is used for heat exchange between the air inlet pipeline (10) and the middle pipeline (L), and the heat exchanger B (6) is used for heat exchange between the air outlet pipeline (20) and the middle pipeline (L).
3. The deep purification system for hydrocarbons according to claim 1, wherein: the heat exchange module comprises at least one heat exchanger A (5) and at least one heat exchanger B (6), the heat exchanger A (5) and the heat exchanger B (6) are sequentially arranged on a gas outlet pipeline (20) of the high-temperature reactor (2), and the heat exchanger B (6) is positioned at the upstream of the heat exchanger A (5);
the heat exchanger A (5) is used for heat exchange between the air inlet pipeline (10) and the air outlet pipeline (20), and the heat exchanger B (6) is used for heat exchange between the middle pipeline (L) and the air outlet pipeline (20).
4. The deep purification system for hydrocarbons according to claim 1, wherein: the heat exchange module comprises at least one heat exchanger A (5), at least one heat exchanger B (6) and at least one heat exchanger C (7), the heat exchanger A (5), the heat exchanger C (7) and the heat exchanger B (6) are sequentially arranged on the intermediate pipeline (L), and the heat exchanger A (5) is close to the gas outlet of the low-temperature reactor (1);
the heat exchanger A (5) is used for heat exchange between the air inlet pipeline (10) and the middle pipeline (L), and the heat exchanger B (6) and the heat exchanger C (7) are both used for heat exchange between the air outlet pipeline (20) and the middle pipeline (L).
5. The deep purification system for hydrocarbons according to any one of claims 1 to 4, wherein: the first heater (3) and the second heater (4) are external heaters arranged on pipelines, and/or heating structures arranged inside the reactor, and/or heating structures arranged on the outer wall of the reactor.
6. The deep purification system for hydrocarbons according to any one of claims 1 to 4, wherein: the second heater (4) is an external heater arranged on the middle pipeline (L), the high-temperature reactor (2) is provided with a third heater (9), and the third heater (9) and the first heater (3) are heating structures extending into the reactor or attached to the outer wall of the reactor.
7. The deep purification system for hydrocarbons according to claim 1, wherein: and temperature sensors (T) are arranged on the low-temperature reactor (1) and the high-temperature reactor (2).
8. The deep purification system for hydrocarbons according to claim 1, wherein: the heat exchange module is detachably arranged on the pipeline and/or integrated on the cylinders of the low-temperature reactor (1) and the high-temperature reactor (2).
9. The deep purification system for hydrocarbons according to any one of claims 1 to 4, wherein: and the air inlet pipeline (10) and/or the air outlet pipeline (20) are/is provided with a stop valve (8).
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| CN111871195A (en) * | 2020-07-27 | 2020-11-03 | 重庆鲍斯净化设备科技有限公司 | Hydrocarbon compound deep purification system |
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| CN111871195A (en) * | 2020-07-27 | 2020-11-03 | 重庆鲍斯净化设备科技有限公司 | Hydrocarbon compound deep purification system |
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