CN220546778U - Gas recovery system - Google Patents
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- CN220546778U CN220546778U CN202320664441.6U CN202320664441U CN220546778U CN 220546778 U CN220546778 U CN 220546778U CN 202320664441 U CN202320664441 U CN 202320664441U CN 220546778 U CN220546778 U CN 220546778U
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- 238000011084 recovery Methods 0.000 title claims abstract description 47
- 238000001179 sorption measurement Methods 0.000 claims abstract description 422
- 230000007246 mechanism Effects 0.000 claims abstract description 236
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 86
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 39
- 239000012535 impurity Substances 0.000 claims abstract description 39
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 25
- 239000004215 Carbon black (E152) Substances 0.000 claims abstract description 24
- 238000000034 method Methods 0.000 claims abstract description 21
- 238000004227 thermal cracking Methods 0.000 claims abstract description 16
- 238000006243 chemical reaction Methods 0.000 claims abstract description 15
- 239000007789 gas Substances 0.000 claims description 233
- 239000001257 hydrogen Substances 0.000 claims description 31
- 229910052739 hydrogen Inorganic materials 0.000 claims description 31
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 30
- 238000003795 desorption Methods 0.000 claims description 26
- 238000010438 heat treatment Methods 0.000 claims description 9
- 238000007599 discharging Methods 0.000 claims description 4
- 238000005086 pumping Methods 0.000 claims description 2
- 229910052799 carbon Inorganic materials 0.000 abstract description 40
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 30
- -1 carbon hydrocarbon Chemical class 0.000 abstract description 11
- 238000004519 manufacturing process Methods 0.000 abstract description 11
- 239000002131 composite material Substances 0.000 abstract description 8
- 238000000746 purification Methods 0.000 abstract description 5
- 230000007613 environmental effect Effects 0.000 abstract description 4
- 239000002699 waste material Substances 0.000 abstract description 4
- 238000002360 preparation method Methods 0.000 abstract description 3
- CREMABGTGYGIQB-UHFFFAOYSA-N carbon carbon Chemical compound C.C CREMABGTGYGIQB-UHFFFAOYSA-N 0.000 abstract description 2
- 239000011203 carbon fibre reinforced carbon Substances 0.000 abstract description 2
- 239000003463 adsorbent Substances 0.000 description 27
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 16
- 238000005229 chemical vapour deposition Methods 0.000 description 10
- 229910052757 nitrogen Inorganic materials 0.000 description 8
- 230000008569 process Effects 0.000 description 7
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 5
- 239000002245 particle Substances 0.000 description 5
- 239000013078 crystal Substances 0.000 description 4
- 239000013067 intermediate product Substances 0.000 description 4
- 230000009471 action Effects 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 229920006395 saturated elastomer Polymers 0.000 description 3
- 238000002485 combustion reaction Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000002808 molecular sieve Substances 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 150000001721 carbon Chemical class 0.000 description 1
- 238000004590 computer program Methods 0.000 description 1
- 238000000151 deposition Methods 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000000543 intermediate Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000002296 pyrolytic carbon Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000000741 silica gel Substances 0.000 description 1
- 229910002027 silica gel Inorganic materials 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
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- Separation Of Gases By Adsorption (AREA)
Abstract
The utility model relates to the field of carbon-carbon composite material preparation, in particular to a gas recovery system. The gas recovery system comprises a first adsorption mechanism for removing impurities in tail gas of thermal cracking reaction of carbon hydrocarbon gas and a second adsorption mechanism for recovering methane gas in the tail gas; the first adsorption mechanism and the second adsorption mechanism are sequentially connected, and tail gas of the thermal cracking reaction of the carbon hydrocarbon gas sequentially passes through the first adsorption mechanism and the second adsorption mechanism; and the second adsorption mechanism recovers methane through a pressure swing adsorption method. The tail gas of hydrocarbon gaseous thermal cracking reaction loops through first adsorption device, second adsorption device, adsorbs the impurity in the tail gas when passing through first adsorption device, and through pressure swing adsorption method recovery methane when passing through the second adsorption device, gas recovery system can realize the purification and the recovery of methane to tail gas for tail gas emission is more environmental protection, but also can avoid the waste of carbon-containing hydrocarbon, practices thrift manufacturing cost.
Description
Technical Field
The utility model relates to the field of carbon-carbon composite material preparation, in particular to a gas recovery system.
Background
The preparation process of the single crystal is mainly a Czochralski method, and the process of preparing the single crystal by the Czochralski method is carried out in a single crystal furnace. The single crystal furnace is provided with a thermal field material piece such as a crucible, a heating element and the like, and the thermal field material piece can be made of a carbon/carbon composite material.
The production of carbon/carbon composites generally employs chemical vapor deposition, which uses thermal cracking of hydrocarbon-containing gases to obtain pyrolytic carbon, which is densified by deposition on pre-woven preforms to obtain carbon/carbon green bodies of desired density. In the production process of the carbon/carbon composite material, the thermal cracking reaction of the carbon hydrocarbon gas is insufficient, and the discharged tail gas also contains a large amount of feed gas.
In the prior art, tail gas is combusted or directly emptied, which is not beneficial to environmental protection, and raw gas is wasted, so that certain economic loss is caused.
Disclosure of Invention
In view of this, the present utility model aims to provide a gas recovery system to solve or partially solve the problems of the existing combustion or direct evacuation treatment of tail gas, adverse environmental protection, waste of raw gas, and certain economic loss.
In order to achieve the above purpose, the technical scheme of the utility model is realized as follows:
the embodiment of the utility model provides a gas recovery system, which comprises a first adsorption mechanism for removing impurities in tail gas of a thermal cracking reaction of carbon hydrocarbon gas and a second adsorption mechanism for recovering methane gas in the tail gas; the first adsorption mechanism and the second adsorption mechanism are sequentially connected, and tail gas of the thermal cracking reaction of the carbon hydrocarbon gas sequentially passes through the first adsorption mechanism and the second adsorption mechanism; and the second adsorption mechanism recovers methane through a pressure swing adsorption method.
Optionally, the second adsorption mechanism comprises a plurality of pressure swing adsorption towers and a second switch controller, and the pressure swing adsorption towers are connected in parallel; the second switch controller is connected with the pressure swing adsorption tower and is used for controlling the connection or disconnection of the gas inlet and the gas outlet of the pressure swing adsorption tower.
Optionally, when at least one of the pressure swing adsorption towers is in an adsorption state, the other pressure swing adsorption tower is in a desorption state.
Optionally, the second adsorption mechanism further comprises a vacuum pump, an air inlet of the vacuum pump is connected with the first air outlet of the second adsorption mechanism, and the second adsorption mechanism performs desorption through vacuum pumping.
Optionally, the first adsorption mechanism comprises a plurality of temperature swing adsorption towers and a first switch controller, and the temperature swing adsorption towers are connected in parallel; the first switch controller is connected with the temperature swing adsorption tower and is used for controlling the connection or disconnection of the gas inlet and the gas outlet of the temperature swing adsorption tower.
Optionally, when at least one of the temperature swing adsorption towers is in an adsorption state, the other temperature swing adsorption tower is in a desorption state.
Optionally, the second air outlet of the second adsorption mechanism is connected with the second air inlet of the first adsorption mechanism; the second gas outlet of the second adsorption mechanism is used for discharging hydrogen-rich gas, the second gas inlet of the first adsorption mechanism is used for flowing in the hydrogen-rich gas, and the first adsorption mechanism uses the hydrogen-rich gas as analysis gas.
Optionally, the first adsorption mechanism comprises a heater, an air inlet of the heater is connected with a second air outlet of the second adsorption mechanism, and an air outlet of the heater is connected with a second air inlet of the first adsorption mechanism; the heater is used for heating the hydrogen-rich gas.
Optionally, a heating unit and a temperature adjusting unit are arranged in the temperature swing adsorption tower, and the temperature adjusting unit is used for adjusting the heat applied by the heating unit to the temperature swing adsorption tower so as to realize the adsorption or desorption of impurities by the temperature swing adsorption tower.
Optionally, the gas recovery system further comprises a first compressor, the first compressor being configured to compress the tail gas; the tail gas sequentially passes through the first compressor, the first adsorption mechanism and the second adsorption mechanism; or the tail gas sequentially passes through the first adsorption mechanism, the first compressor and the second adsorption mechanism.
Optionally, the gas recovery system further comprises a second compressor, the second compressor is connected with the second adsorption mechanism, and the second compressor is used for compressing methane gas discharged from the second adsorption mechanism.
Optionally, the gas recovery system further comprises a filter, the filter is connected with the first adsorption mechanism, and the tail gas sequentially passes through the filter and the first adsorption mechanism.
In the gas recovery system disclosed by the utility model, the tail gas of the thermal cracking reaction of the carbon hydrocarbon gas sequentially passes through the first adsorption mechanism and the second adsorption mechanism, impurities in the tail gas are adsorbed when passing through the first adsorption mechanism, and methane is recovered by a pressure swing adsorption method when passing through the second adsorption mechanism, so that the gas recovery system can realize the purification of the tail gas and the recovery of methane, the tail gas emission is more environment-friendly, the waste of carbon hydrocarbon can be avoided, and the production cost is saved.
The foregoing description is only an overview of the present utility model, and is intended to be implemented in accordance with the teachings of the present utility model in order that the same may be more clearly understood and to make the same and other objects, features and advantages of the present utility model more readily apparent.
Drawings
In order to more clearly illustrate the embodiments of the present utility model or the technical solutions in the prior art, the drawings used in the description of the embodiments will be briefly described below.
FIG. 1 is a schematic diagram of a gas recovery system according to an embodiment of the present utility model;
fig. 2 is a schematic diagram of a gas recovery system according to another embodiment of the present utility model.
Reference numerals illustrate:
10-a first adsorption mechanism; 11-a first air inlet of a first adsorption mechanism; 12-a second air inlet of the first adsorption mechanism; 13-a first air outlet of the first adsorption mechanism; 14-a second air outlet of the first adsorption mechanism; 15-a heater; 16-a temperature swing adsorption column;
20-a second adsorption mechanism; 21-a first air inlet of a second adsorption mechanism; 22-a first air outlet of a second adsorption mechanism; 23-a second air outlet of the second adsorption mechanism; 24-a first compressor; 25-a vacuum pump; 26-a pressure swing adsorption column; 27-compressor.
Detailed Description
Exemplary embodiments of the present utility model will be described in more detail below with reference to the accompanying drawings. While exemplary embodiments of the present utility model are shown in the drawings, it should be understood that the present utility model may be embodied in various forms and should not be limited to the embodiments set forth herein. Rather, these embodiments are provided so that this disclosure will be thorough and complete, and will fully convey the scope of the utility model to those skilled in the art.
Referring to fig. 1, a schematic structural diagram of a gas recovery system according to an embodiment of the present utility model is shown, where the gas recovery system is mainly used for recovering gas, and the embodiment of the present utility model is not limited to gas. For example, the gas is an off-gas generated during chemical vapor deposition. In the chemical vapor deposition process, when the thermal cracking reaction of the hydrocarbon gas is insufficient, the discharged tail gas contains recoverable gas. The tail gas components of the thermal cracking reaction of the carbon hydrocarbon gas are complex, and most of the tail gas components are hydrocarbons, nitrogen, hydrogen and the like, wherein the carbon-containing hydrocarbon and the hydrogen account for more than 90 percent. The components of the recoverable gas in the tail gas mainly comprise methane, a small amount of low-carbon hydrocarbon such as ethane and the like; impurities in the tail gas include carbon particles which may exist, long-chain hydrocarbons volatilized by vacuum pump oil, and chain hydrocarbons of intermediate products of chemical vapor deposition; the tail gas also comprises non-adsorbable gases such as nitrogen, hydrogen and the like. The low-carbon hydrocarbon such as methane and ethane in the tail gas is recovered through the gas recovery system and is continuously used after recovery, so that the problem of high carbon emission of chemical vapor deposition is solved, the utilization rate of the carbon hydrocarbon gas is improved, and the production cost of chemical vapor deposition is reduced.
Referring to fig. 1, the gas recovery system includes a first adsorption mechanism 10 and a second adsorption mechanism 20; the first adsorption mechanism 10 is used for removing impurities in tail gas of a thermal cracking reaction of the carbon hydrocarbon gas, the first air inlet 11 of the first adsorption mechanism is used for flowing in the tail gas, the first air outlet 13 of the first adsorption mechanism is connected with the first air inlet 21 of the second adsorption mechanism, and the tail gas of the thermal cracking reaction of the carbon hydrocarbon gas sequentially passes through the first adsorption mechanism 10 and the second adsorption mechanism 20; the second adsorption mechanism 20 is used for recovering methane gas in the tail gas, specifically, the second adsorption mechanism 20 recovers methane gas by a pressure swing adsorption method, and the recovered methane is discharged through a first gas outlet 22 of the second adsorption mechanism.
Specifically, the first adsorption mechanism 10 includes a first air inlet 11 of the first adsorption mechanism and a first air outlet 13 of the first adsorption mechanism. The first air inlet 11 of the first adsorption mechanism is used for flowing in the tail gas of the thermal cracking reaction of the hydrocarbon gas, impurities in the tail gas are adsorbed in the first adsorption mechanism 10, and the clean tail gas after the impurities are adsorbed flows out through the first air outlet 13 of the first adsorption mechanism. The first adsorption mechanism 10 can realize purification of exhaust gas. Wherein the impurities include at least one of carbon particles, long-chain hydrocarbons volatilized from vacuum pump oil, and chain hydrocarbons of chemical vapor deposition intermediates.
The second adsorption mechanism 20 comprises a first air inlet 21 of the second adsorption mechanism and a first air outlet 22 of the second adsorption mechanism, and clean tail gas after impurities are adsorbed flows into the second adsorption mechanism 20 through the first air inlet 21 of the second adsorption mechanism. The second adsorption means 20 is for adsorbing a recoverable gas mainly comprising methane and a small amount of lower hydrocarbons such as ethane contained in the exhaust gas, the second adsorption means 20 is mainly for adsorbing methane gas, non-adsorbable gases such as nitrogen and hydrogen in the exhaust gas are discharged through the second gas outlet 23 of the second adsorption means, and the recoverable gas desorbed from the second adsorption means 20 is discharged through the first gas outlet 22 of the second adsorption means.
In sum, in the gas recovery system of this application embodiment, the tail gas of hydrocarbon gas thermal cracking reaction loops through first adsorption mechanism 10, second adsorption mechanism 20, adsorb the impurity in the tail gas when tail gas passes through first adsorption mechanism 10, pass through pressure swing adsorption method recovery methane when tail gas passes through second adsorption mechanism 20, gas recovery system can realize purifying and the recovery of methane to the tail gas for exhaust emission is more environmental protection, but also can avoid the waste of carbon-containing hydrocarbon, practices thrift manufacturing cost.
Optionally, the first adsorption mechanism 10 includes a plurality of temperature swing adsorption towers 16 and a first switch controller, and the plurality of temperature swing adsorption towers 16 are connected in parallel; the first switch controller is connected with the temperature swing adsorption tower 16, and the first switch controller is used for controlling the connection or disconnection of the gas inlet and the gas outlet of the temperature swing adsorption tower 16. With further reference to fig. 1, the first switch controller is configured to control the temperature swing adsorption tower 16 to be turned on or off from the first air inlet 11 of the first adsorption mechanism, the first air outlet 13 of the first adsorption mechanism, the second air inlet 12 of the first adsorption mechanism, and the second air outlet 14 of the first adsorption mechanism.
Specifically, when the plurality of temperature swing adsorption towers 16 are arranged in parallel, any one of the temperature swing adsorption towers 16 does not affect the other temperature swing adsorption towers 16 when performing adsorption or desorption. Wherein the plurality of temperature swing adsorption columns 16 refers to at least two temperature swing adsorption columns 16.
In order to increase the treatment efficiency, at least one of the temperature swing adsorption towers 16 is in an adsorption state while the other is in a desorption state. I.e., portions of the plurality of temperature swing adsorption columns 16 are used to adsorb impurities, a plurality of variations
The remainder of the warm adsorption column 16 is used to desorb impurities. For example, when the first adsorption mechanism 10 includes two temperature swing adsorption columns 16, one temperature swing adsorption column 16 is used to adsorb impurities and the other temperature swing adsorption column 16 is used to desorb impurities, which are defined as a first temperature swing adsorption column and a second temperature swing adsorption column, respectively. The working processes of adsorption by one temperature swing adsorption tower and desorption by the other temperature swing adsorption tower can be as follows:
when the first switch controller controls the first temperature swing adsorption tower to be connected with the first air inlet 11 of the first adsorption mechanism and the first air outlet 13 of the first adsorption mechanism and disconnected with the second air inlet 12 of the first adsorption mechanism and the second air outlet 14 of the first adsorption mechanism, the first temperature swing adsorption tower adsorbs impurities; at this time, the first switch controller controls the second temperature swing adsorption tower to be connected to the second air inlet 12 of the first adsorption mechanism and the second air outlet 14 of the first adsorption mechanism, and disconnected from the first air inlet 11 of the first adsorption mechanism and the first air outlet 13 of the first adsorption mechanism, and the second temperature swing adsorption tower is used for desorbing impurities. When the first switch controller controls the first temperature swing adsorption tower to be connected with the second air inlet 12 of the first adsorption mechanism and the second air outlet 14 of the first adsorption mechanism and disconnected with the first air inlet 11 of the first adsorption mechanism and the first air outlet 13 of the first adsorption mechanism, the first temperature swing adsorption tower is used for desorbing impurities; at this time, the first switch controller controls the second temperature swing adsorption tower to be connected to the first air inlet 11 of the first adsorption mechanism and the first air outlet 13 of the first adsorption mechanism, and disconnected from the second air inlet 12 of the first adsorption mechanism and the second air outlet 14 of the first adsorption mechanism, and the second temperature swing adsorption tower adsorbs impurities.
Optionally, the first switch controller includes a control unit and a control valve, and the control unit controls opening or closing of the control valve.
The temperature swing adsorption tower 16 is connected with the first air inlet 11 of the first adsorption mechanism, the second air inlet 12 of the first adsorption mechanism, the first air outlet 13 of the first adsorption mechanism and the second air outlet 14 of the first adsorption mechanism through air pipes, and the control valve can be arranged on the air pipes.
Optionally, one end of the temperature swing adsorption tower 16 is connected with the first air outlet 13 of the first adsorption mechanism, and the other end of the temperature swing adsorption tower 16 is connected with the first air inlet 11 of the first adsorption mechanism, the second air inlet 12 of the first adsorption mechanism and the second air outlet 14 of the first adsorption mechanism.
Referring further to fig. 1, the top of the temperature swing adsorption tower 16 is connected to the first air outlet 13 of the first adsorption mechanism, and the bottom of the temperature swing adsorption tower 16 is connected to the first air inlet 11 of the first adsorption mechanism, the second air inlet 12 of the first adsorption mechanism, and the second air outlet 14 of the first adsorption mechanism. It can be understood that the connection positions of the temperature swing adsorption tower 16 and the first air outlet 13 of the first adsorption mechanism, the first air inlet 11 of the first adsorption mechanism, the second air inlet 12 of the first adsorption mechanism, and the second air outlet 14 of the first adsorption mechanism are set according to the use requirements, which is not specifically limited in this embodiment of the present application.
Optionally, the second air inlet 12 of the first adsorption mechanism is connected with the second air outlet 23 of the second adsorption mechanism; the second gas outlet 23 of the second adsorption mechanism is used for discharging non-adsorbable gas in the tail gas, which includes hydrogen or sometimes includes hydrogen and nitrogen; wherein, the hydrogen content is higher. Therefore, the second air outlet 23 of the second adsorption mechanism is mainly used for discharging the hydrogen-rich gas, and the first adsorption machine
The second gas inlet 12 is configured to flow in hydrogen-rich gas, and the first adsorption mechanism uses the hydrogen-rich gas as the desorption gas. The hydrogen-rich gas discharged from the second gas outlet 23 of the second adsorption mechanism is used as the desorption gas, so that the gas can be recycled.
Optionally, the first adsorption mechanism 10 further includes a heater 15, an air inlet of the heater 15 is connected with the second air outlet 23 of the second adsorption mechanism, and an air outlet of the heater 15 is connected with the second air inlet 12 of the first adsorption mechanism; the heater 15 is used to heat the hydrogen rich gas.
Specifically, the hydrogen-rich gas flowing out from the second gas outlet 23 of the second adsorption mechanism enters the heater 15 through the gas inlet of the heater 15, the heater 15 heats the hydrogen-rich gas, the heated high-temperature hydrogen-rich gas flows out from the gas outlet of the heater 15 as desorption gas and flows into the first adsorption mechanism 10 through the second gas inlet 12 of the first adsorption mechanism, after contacting with the temperature-changing adsorbent in the first adsorption mechanism 10, the temperature-changing adsorbent releases impurities, and the impurities and the desorption gas are discharged from the second gas outlet 14 of the first adsorption mechanism together. After the temperature-changing adsorbent releases impurities, the temperature-changing adsorbent can be used for adsorbing the impurities again, so that the recycling is realized.
It will be appreciated that the type of temperature swing adsorbent is compatible with the impurities to be adsorbed, and that the temperature swing adsorbent in the embodiments herein is not limited, and for example, the temperature swing adsorbent comprises at least one of a carbon molecular sieve, activated carbon, and porous alumina.
The first adsorption mechanism 10 is a temperature swing adsorption mechanism, and the temperature swing adsorbent adsorbs impurities at normal temperature and desorbs the impurities at high temperature. Wherein, the normal temperature is 10 ℃ to 40 ℃, and the temperature-variable adsorbent has stronger adsorption effect on impurities at 10 ℃ to 40 ℃. The high temperature is, for example, 150 ℃ to 200 ℃, and the temperature swing adsorbent can desorb at 150 ℃ to 200 ℃.
Optionally, a heating unit and a temperature adjusting unit are arranged in the temperature swing adsorption tower 16, and the temperature adjusting unit adjusts the heat applied to the temperature swing adsorption tower by the heating unit to realize the adsorption or desorption of impurities by the temperature swing adsorption tower.
Further, the impurities and the desorbed gas are discharged together from the second gas outlet 14 of the first adsorption mechanism, and then can be sent to a tail gas treatment system for subsequent treatment, for example, combustion and the like.
In one embodiment, referring to FIG. 1, the gas recovery system further includes a first compressor 24, the first compressor 24 for compressing the tail gas; the exhaust gas passes through the first compressor 24, the first adsorption mechanism 10, and the second adsorption mechanism 20 in this order. At this time, the air outlet of the first compressor 24 is connected to the first air inlet 11 of the first adsorption mechanism.
Specifically, the first compressor 24 is used for pressurizing the tail gas, the tail gas flowing out from the air outlet of the first compressor 24 is high-pressure tail gas, the high-pressure tail gas enters the first adsorption mechanism 10 through the first air inlet 11 of the first adsorption mechanism, the tail gas discharged from the first air outlet 13 of the first adsorption mechanism is purified high-pressure tail gas, the purified high-pressure tail gas enters the second adsorption mechanism 20 through the first air inlet 21 of the second adsorption mechanism, and the pressure swing adsorbent in the second adsorption mechanism 20 is used for purifying the first and second high-pressure tail gas
The alkane is adsorbed.
In another embodiment, referring to fig. 2, the exhaust gas passes through the first adsorption mechanism 10, the first compressor 24, and the second adsorption mechanism 20 in that order. At this time, the air inlet of the first compressor 24 is connected to the first air outlet 13 of the first adsorption mechanism, and the air outlet of the first compressor 24 is connected to the first air inlet 21 of the second adsorption mechanism.
At this time, the first compressor 24 is also used for pressurizing the tail gas, the purified clean tail gas discharged from the first air outlet 13 of the first adsorption mechanism enters the first compressor 24 through the air inlet of the first compressor 24, the first compressor 24 pressurizes the tail gas, the pressurized high-pressure tail gas flows out from the air outlet of the first compressor 24 and enters the second adsorption mechanism 20 through the first air inlet 21 of the second adsorption mechanism, and the pressure swing adsorbent in the second adsorption mechanism 20 adsorbs methane in the high-pressure tail gas.
The first compressor 24 generally pressurizes the tail gas to 0.3MPa to 1.5MPa, and is specifically set according to the use requirement.
The second adsorption mechanism 20 is a pressure swing adsorption mechanism, and the pressure swing adsorbent adsorbs methane at high pressure. The first compressor 24 pressurizes the tail gas, so that methane in the tail gas can be better adsorbed in the second adsorption mechanism 20; when the first compressor 24 is disposed upstream of the first adsorption mechanism 10, with further reference to fig. 1, the first compressor 24 also enables steady operation of the exhaust gas in the overall system; after compressing the volume of the tail gas, the volume of each reactor, gas vessel, etc. at the back end may be reduced, for example, by reducing the volume of temperature swing adsorption column 16, pressure swing adsorption column 26, etc. at the back end.
Optionally, the second adsorption mechanism 20 includes a plurality of pressure swing adsorption towers 26 and a second switch controller, and the plurality of pressure swing adsorption towers 26 are connected in parallel; the second switch controller is connected with the pressure swing adsorption tower 26, and is used for controlling the connection or disconnection of the gas inlet and the gas outlet of the pressure swing adsorption tower 26. With further reference to fig. 1, the second switch controller controls the pressure swing adsorption tower 26 to be turned on or off with the first air inlet 21 of the second adsorption mechanism, the first air outlet 22 of the second adsorption mechanism, and the second air outlet 23 of the second adsorption mechanism.
Specifically, when the plurality of pressure swing adsorption towers 26 are arranged in parallel, any one pressure swing adsorption tower 26 is not affected by other pressure swing adsorption towers 26 when adsorption or desorption is performed. Wherein the plurality of pressure swing adsorption columns 26 refers to at least two temperature swing adsorption columns 16.
In order to improve the treatment efficiency, at least one of the pressure swing adsorption towers 26 is in an adsorption state, and the other is in a desorption state. That is, a part of the plurality of pressure swing adsorption columns 26 is used for adsorption recovery of methane, and the remaining part of the plurality of pressure swing adsorption columns 26 is used for desorption of methane. For example, when the second adsorption mechanism 20 includes two pressure swing adsorption columns 26, one pressure swing adsorption column 26 is used for adsorbing methane, and the other pressure swing adsorption column 26 is used for desorbing, which are defined as a first pressure swing adsorption column and a second pressure swing adsorption column, respectively. The working processes of adsorption by one pressure swing adsorption tower and desorption by the other pressure swing adsorption tower can be as follows:
when the second switch controller controls the first pressure swing adsorption tower and the first air inlet of the second adsorption mechanism
21 are connected with a second air outlet 23 of the second adsorption mechanism, and when the second air outlet is disconnected with a first air outlet 22 of the second adsorption mechanism, the first pressure swing adsorption tower adsorbs methane; at this time, the second switch controller controls the second pressure swing adsorption tower to be connected with the first air outlet 22 of the second adsorption mechanism, disconnected with the first air inlet 21 of the second adsorption mechanism and the second air outlet 23 of the second adsorption mechanism, and the second pressure swing adsorption tower desorbs methane. When the second switch controller controls the first pressure swing adsorption tower to be connected with the first air outlet 22 of the second adsorption mechanism and disconnected with the first air inlet 21 of the second adsorption mechanism and the second air outlet 23 of the second adsorption mechanism, the first pressure swing adsorption tower is used for desorbing methane; at this time, the second switch controller controls the second pressure swing adsorption tower to be connected to the first air inlet 21 of the second adsorption mechanism and the second air outlet 23 of the second adsorption mechanism, disconnected from the first air outlet 22 of the second adsorption mechanism, and the second pressure swing adsorption tower adsorbs methane. The desorbed methane flows out through the first gas outlet 22 of the second adsorption mechanism.
Optionally, the second switch controller also includes a control unit and a control valve, and the control unit controls the opening or closing of the control valve. The pressure swing adsorption tower 26 is connected with the first air inlet 21 of the second adsorption mechanism, the second air outlet 23 of the second adsorption mechanism and the first air outlet 22 of the second adsorption mechanism through air pipes, and the control valve can be arranged on the air pipes.
Alternatively, referring to fig. 1, one end of the pressure swing adsorption tower 26 is connected to the second air outlet 23 of the second adsorption mechanism, and the other end of the pressure swing adsorption tower 26 is connected to the first air inlet 21 of the second adsorption mechanism and the first air outlet 22 of the second adsorption mechanism.
Referring further to fig. 1, the top of the pressure swing adsorption tower 26 is connected to the second air outlet 23 of the second adsorption mechanism, and the bottom of the pressure swing adsorption tower 26 is connected to the first air inlet 21 of the second adsorption mechanism and the first air outlet 22 of the second adsorption mechanism. It can be understood that the connection positions of the pressure swing adsorption tower 26 and the first air inlet 21 of the second adsorption mechanism, the first air outlet 22 of the second adsorption mechanism, and the second air outlet 23 of the second adsorption mechanism are set according to the use requirement, which is not particularly limited in the embodiment of the present application.
In an embodiment, referring to fig. 1, the second adsorption mechanism 20 further includes a vacuum pump 25, an air inlet of the vacuum pump 25 is connected to the first air outlet 22 of the second adsorption mechanism, and the second adsorption mechanism performs desorption by vacuumizing through the vacuum pump 25. The vacuum pump 25 is used for vacuumizing to reduce the air pressure in the pressure swing adsorption tower 26, the pressure swing adsorbent in the pressure swing adsorption tower 26 desorbs methane, and the methane is pumped out of the pressure swing adsorption tower 26 by the vacuum pump 25.
The pressure swing adsorbent is desorbed by vacuum pump 25 to vacuum pressure swing adsorption tower 26, and has high desorption speed, no other gas and no new impurity to desorbed methane.
In another embodiment, the second adsorption mechanism 20 may not be provided with a vacuum pump 25, the pressure swing adsorbent in the pressure swing adsorption tower 26 may be desorbed under normal pressure, and the desorbed raw gas is discharged through the first gas outlet 22 of the second adsorption mechanism.
It will be appreciated that the pressure swing adsorbent is of a type that matches the type of impurities adsorbed, embodiments of the present application
The pressure swing adsorbent is not limited, and for example, the pressure swing adsorbent includes one or more of carbon molecular sieve, activated carbon and silica gel.
Alternatively, the number of pressure swing adsorption columns 26 is even. At this time, one half of the pressure swing adsorption towers 26 are used for adsorption, the other half of the pressure swing adsorption towers 26 are used for desorption, and the gas recovery system can balance the desorption and the adsorption.
Optionally, the gas recovery system further comprises a second compressor 27, and an air inlet of the second compressor 27 is connected to an air outlet of the vacuum pump 25. The second compressor 27 compresses the methane discharged from the first air outlet 22 of the second adsorption mechanism to pressurize the methane, and the pressurized methane can meet the air pressure requirement when the methane participates in production again, or reduce the space of the storage container when the methane is stored.
Optionally, the gas recovery system further comprises a filter, the filter is connected with the first adsorption mechanism 10, and the tail gas sequentially passes through the filter and the first adsorption mechanism 10. The filter can filter tail gas for the tail gas is cleaner.
In the above gas recovery system, the first adsorption mechanism 10 is a temperature swing adsorption mechanism, and the second adsorption mechanism 20 is a pressure swing adsorption mechanism, and it can be understood that in practical application, the first adsorption mechanism 10 and the second adsorption mechanism 20 may be temperature swing adsorption mechanisms, and the first adsorption mechanism 10 and the second adsorption mechanism 20 may also be pressure swing adsorption mechanisms, which are specifically designed according to the use requirements.
In one embodiment, the gas recovery system is used for treating tail gas from a carbon/carbon composite production process, for example:
the components of the tail gas discharged in the production process of the carbon/carbon composite material are more complex, and most of the components are hydrocarbons, nitrogen, hydrogen and the like, wherein the proportion of the carbon-containing hydrocarbon to the hydrogen is more than 90%, the components to be recovered are methane, a small amount of ethane and other low-carbon hydrocarbons contained in the tail gas, the carbon particles possibly existing, long-chain hydrocarbons volatilized by vacuum pump oil, the chain hydrocarbons of chemical vapor deposition intermediate products, and the nitrogen and the hydrogen are separated from the tail gas, and the gas recovery system simultaneously uses a temperature swing adsorption mode and a pressure swing adsorption mode to treat the discharged tail gas.
Referring to fig. 1, the exhaust gas discharged during the production of the carbon/carbon composite material is first introduced into the first compressor 24, the pressure of the exhaust gas is increased by the first compressor 24, and the pressurized high-pressure exhaust gas discharged from the gas outlet of the first compressor 24 is introduced into the temperature swing adsorption tower 16 through the first gas inlet 11 of the first adsorption mechanism. The temperature swing adsorption tower 16 is mainly used for removing carbon particles possibly existing in the high-pressure tail gas, long-chain hydrocarbons volatilized by vacuum pump oil and chain hydrocarbons of intermediate products of chemical vapor deposition. The purified high-pressure tail gas is discharged through a first air outlet 13 of the first adsorption mechanism and then enters a pressure swing adsorption tower 26 through a first air inlet 21 of the second adsorption mechanism; the pressure swing adsorbent in the pressure swing adsorption tower 26 has a strong adsorption effect on recoverable gas in high-pressure tail gas, but hardly adsorbs nitrogen and hydrogen, and after the high-pressure tail gas enters the pressure swing adsorption tower 26, the recoverable gas is adsorbed by the pressure swing adsorbent, and the non-adsorbable nitrogen and hydrogen are discharged from the second gas outlet 23 of the second adsorption mechanism at the top of the pressure swing adsorption tower 26 to form hydrogen-rich gas. Wherein the recoverable gas mainly comprises methane and tail gas
Small amounts of lower hydrocarbons such as ethane.
After the pressure swing adsorption tower 26 is saturated by adsorption, the pressure swing adsorption tower 26 is subjected to depressurization treatment by the vacuum pump 25, the pressure swing adsorption tower 26 is desorbed in a low-pressure state, the recyclable gas is discharged from the first gas outlet 22 of the second adsorption mechanism, and the discharged recyclable gas is pressurized by the raw gas compressor 27 and then sent back to the carbon/carbon composite material production plant for continuous use. After the pressure swing adsorbent desorbs the recoverable gas and the recoverable gas is vented, the pressure swing adsorbent in pressure swing adsorption column 26 resumes an adsorbable state.
After the temperature swing adsorbent of the temperature swing adsorption column 16 is saturated, the high pressure tail gas stops entering the temperature swing adsorption column 16 saturated with adsorption. The non-adsorbable hydrogen-rich gas discharged from the pressure swing adsorption tower 26 through the second gas outlet 23 of the second adsorption mechanism is heated by the heater 15, and then returned to the temperature swing adsorption tower 16 through the second gas inlet 12 of the first adsorption mechanism, and the heated hydrogen-rich gas is used as a desorption gas to desorb impurities from the temperature swing adsorbent in the temperature swing adsorption tower 16, the impurities and the non-adsorbable gas are discharged from the temperature swing adsorption tower 16 through the second gas outlet 14 of the first adsorption mechanism, and the temperature swing adsorbent in the temperature swing adsorption tower 16 is recovered to an adsorbable state after the impurities are discharged.
In the above-described flow, the first compressor 24 pressurizes the exhaust gas to 0.3 to 1.5MPa, so that the exhaust gas can be better adsorbed in the pressure swing adsorption tower 26.
In the above-mentioned flow, referring to fig. 1, the first adsorption mechanism 10 includes two temperature swing adsorption towers 16, the temperature swing adsorbent filled in the temperature swing adsorption towers 16 has strong adsorption effect on impurities in the tail gas, such as carbon particles, long-chain hydrocarbons volatilized by vacuum pump oil and chain hydrocarbons of chemical vapor deposition intermediate products, and can be desorbed at a temperature of 150-200 ℃, and the desorbed impurity gas can be subjected to subsequent treatment after being discharged from the temperature swing adsorption towers 16.
The temperature swing adsorption towers 16 in the first adsorption mechanism 10 are arranged in double towers, one temperature swing adsorption tower 16 is used for adsorption and purification, the other temperature swing adsorption tower 16 is used for desorption and regeneration, the two temperature swing adsorption towers 16 work circularly and interchangeably in this way, and the continuous purification of tail gas is realized in the first adsorption mechanism 10.
The pressure swing adsorption towers 26 in the second adsorption mechanism 20 are arranged in double towers, one pressure swing adsorption tower 26 is used for adsorption, the other pressure swing adsorption tower 26 is used for desorption and regeneration, the two pressure swing adsorption towers 26 work circularly and interchangeably in this way, and the second adsorption mechanism 20 is used for realizing continuous recovery of methane in tail gas.
It is noted that relational terms such as first and second, and the like are used solely to distinguish one entity or action from another entity or action without necessarily requiring or implying any actual such relationship or order between such entities or actions. Moreover, the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such process, method, article, or apparatus. Without further limitation, an element defined by the phrase "comprising one … …" does not exclude the presence of other like elements in a process, method, article, or apparatus that comprises an element.
In this specification, each embodiment is described in a related manner, and identical and similar parts of each embodiment are all referred to each other, and each embodiment mainly describes differences from other embodiments. For embodiments of an apparatus, an electronic device, a computer-readable storage medium, and a computer program product containing instructions, the description is relatively simple, as it is substantially similar to method embodiments, with reference to the section of the method embodiments being relevant.
The foregoing description is only of the preferred embodiments of the present utility model and is not intended to limit the scope of the present utility model. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present utility model are included in the protection scope of the present utility model.
Claims (11)
1. A gas recovery system, characterized by comprising a first adsorption mechanism (10) for removing impurities in tail gas of a thermal cracking reaction of hydrocarbon gas and a second adsorption mechanism (20) for recovering methane gas in tail gas;
the first adsorption mechanism (10) and the second adsorption mechanism (20) are sequentially connected, and tail gas of the thermal cracking reaction of the hydrocarbon gas sequentially passes through the first adsorption mechanism (10) and the second adsorption mechanism (20); the second adsorption mechanism (20) recovers methane by a pressure swing adsorption method;
a second air outlet (23) of the second adsorption mechanism is connected with a second air inlet (12) of the first adsorption mechanism; the second gas outlet (23) of the second adsorption mechanism is used for discharging hydrogen-rich gas, the second gas inlet (12) of the first adsorption mechanism is used for flowing in the hydrogen-rich gas, and the first adsorption mechanism uses the hydrogen-rich gas as analysis gas.
2. The gas recovery system of claim 1, wherein the second adsorption mechanism (20) comprises a plurality of pressure swing adsorption towers (26) and a second switch controller, a plurality of the pressure swing adsorption towers (26) being connected in parallel; the second switch controller is connected with the pressure swing adsorption tower (26), and is used for controlling the connection or disconnection of an air inlet and an air outlet of the pressure swing adsorption tower (26).
3. The gas recovery system of claim 2, wherein at least one of the pressure swing adsorption towers (26) is in an adsorption state and the other is in a desorption state.
4. The gas recovery system according to claim 2, wherein the second adsorption mechanism (20) further comprises a vacuum pump (25), an air inlet of the vacuum pump (25) being connected to a first air outlet (22) of the second adsorption mechanism, the second adsorption mechanism being desorbed by vacuum-pumping the vacuum pump (25).
5. The gas recovery system of claim 1, wherein the first adsorption mechanism (10) comprises a plurality of temperature swing adsorption columns (16) and a first switch controller, a plurality of the temperature swing adsorption columns (16) being connected in parallel; the first switch controller is connected with the temperature swing adsorption tower (16), and is used for controlling the connection or disconnection of an air inlet and an air outlet of the temperature swing adsorption tower (16).
6. The gas recovery system of claim 5, wherein at least one of said temperature swing adsorption towers (16) is in an adsorption state and the other is in a desorption state.
7. The gas recovery system according to claim 1, wherein the first adsorption mechanism (10) comprises a heater (15), an air inlet of the heater (15) being connected to a second air outlet (23) of the second adsorption mechanism, an air outlet of the heater (15) being connected to a second air inlet (12) of the first adsorption mechanism; the heater (15) is used for heating the hydrogen-rich gas.
8. The gas recovery system according to claim 5, wherein a heating unit and a temperature adjusting unit are provided in the temperature swing adsorption column (16), and heat applied to the temperature swing adsorption column by the heating unit is adjusted by the temperature adjusting unit, thereby realizing adsorption or desorption of the impurities by the temperature swing adsorption column.
9. The gas recovery system according to claim 1, further comprising a first compressor (24), the first compressor (24) being configured to compress the tail gas; the tail gas sequentially passes through the first compressor (24), the first adsorption mechanism (10) and the second adsorption mechanism (20); or,
the tail gas sequentially passes through the first adsorption mechanism (10), the first compressor (24) and the second adsorption mechanism (20).
10. The gas recovery system according to claim 1, further comprising a second compressor (27), the second compressor (27) being connected to the second adsorption means, the second compressor (27) being adapted to compress methane gas exiting the second adsorption means.
11. The gas recovery system according to claim 1, further comprising a filter connected to the first adsorption means (10), the tail gas passing through the filter, the first adsorption means (10) in sequence.
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| CN202320664441.6U CN220546778U (en) | 2023-03-28 | 2023-03-28 | Gas recovery system |
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