CN109173568B - Active carbon level difference adsorption safe concentration method - Google Patents
Active carbon level difference adsorption safe concentration method Download PDFInfo
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- CN109173568B CN109173568B CN201811125089.9A CN201811125089A CN109173568B CN 109173568 B CN109173568 B CN 109173568B CN 201811125089 A CN201811125089 A CN 201811125089A CN 109173568 B CN109173568 B CN 109173568B
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- 238000001179 sorption measurement Methods 0.000 title claims abstract description 71
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title claims abstract description 58
- 238000000034 method Methods 0.000 title claims abstract description 27
- 229910052799 carbon Inorganic materials 0.000 title claims description 10
- 239000007789 gas Substances 0.000 claims abstract description 150
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 59
- 238000003795 desorption Methods 0.000 claims abstract description 57
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 30
- 238000010926 purge Methods 0.000 claims abstract description 20
- 239000006096 absorbing agent Substances 0.000 claims abstract description 13
- 238000000746 purification Methods 0.000 claims abstract description 11
- 239000011261 inert gas Substances 0.000 claims abstract description 7
- 230000008929 regeneration Effects 0.000 claims abstract description 7
- 238000011069 regeneration method Methods 0.000 claims abstract description 7
- 239000000463 material Substances 0.000 claims abstract description 6
- 230000000694 effects Effects 0.000 claims abstract description 5
- 230000008569 process Effects 0.000 claims description 10
- 239000003463 adsorbent Substances 0.000 claims description 9
- 238000001816 cooling Methods 0.000 claims description 9
- 239000003344 environmental pollutant Substances 0.000 claims description 6
- 238000011049 filling Methods 0.000 claims description 6
- 239000012530 fluid Substances 0.000 claims description 6
- 230000003647 oxidation Effects 0.000 claims description 6
- 238000007254 oxidation reaction Methods 0.000 claims description 6
- 231100000719 pollutant Toxicity 0.000 claims description 6
- 238000010438 heat treatment Methods 0.000 claims description 5
- 238000011084 recovery Methods 0.000 claims description 4
- 238000011282 treatment Methods 0.000 claims description 4
- 238000011144 upstream manufacturing Methods 0.000 claims description 3
- 230000008093 supporting effect Effects 0.000 abstract description 3
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 abstract description 2
- 229910021536 Zeolite Inorganic materials 0.000 description 9
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 9
- 239000010457 zeolite Substances 0.000 description 9
- 239000002808 molecular sieve Substances 0.000 description 5
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 5
- 230000002209 hydrophobic effect Effects 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 238000009740 moulding (composite fabrication) Methods 0.000 description 1
- 230000001681 protective effect Effects 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000010408 sweeping Methods 0.000 description 1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
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- Separation Of Gases By Adsorption (AREA)
Abstract
The invention discloses a safe concentration method of activated carbon level difference adsorption.A adsorption device utilizes activated carbon to carry out adsorption and comprises a main adsorber and an auxiliary adsorber; the safety of the main absorber during desorption is improved through nitrogen inert gas protection desorption, so that the regeneration effect of the activated carbon can be improved by improving the nitrogen temperature of the main absorber, and the residual activity of the material after desorption is reduced; after the nitrogen containing high-concentration organic matters discharged by desorption is properly cooled, inert purge gas with lower concentration is formed after the nitrogen is adsorbed and purified by the auxiliary adsorber and is continuously used for high-temperature desorption of the main adsorber, so that the deep desorption work of the main adsorber is completed. The invention designs a combined system of the main adsorber and the auxiliary adsorber by utilizing the characteristic of adsorption balance, and can fully regenerate the main adsorber on the premise of ensuring safety through the adsorption concentration of the level difference and the supporting action of the auxiliary adsorber, thereby ensuring the adsorption purification efficiency of the main adsorber.
Description
Technical Field
The invention belongs to the technical field of environmental protection, relates to a gas purification technology, and particularly relates to a safe concentration method of activated carbon level difference adsorption.
Background
Adsorption concentration is an important means for purifying volatile organic gases, and the current adsorption concentration heating oxidation process becomes a main technical route for purifying low-concentration and large-air-volume organic gases. Since the adsorption, concentration and thermal oxidation process usually uses hot air for desorption, when the adsorbent is combustible activated carbon material, if the temperature of the desorbed hot air is over 100 ℃, the safety problem of fire is easy to occur. The existing reports show that in the concentration heating oxidation process using honeycomb activated carbon as an adsorption material, when air with the temperature higher than 100 ℃ is used for desorption regeneration, a large proportion of the problem of safety of ignition of a carbon layer occurs, and if air with the temperature lower than 100 ℃ is used for desorption of activated carbon which achieves adsorption balance with organic matters with lower concentration in gas, the activated carbon cannot be completely desorbed even if the gas with the same accumulated flow as the adsorption treatment gas is used for purging, so that the residual adsorption capacity of the organic matters in the activated carbon is relatively high, the adsorption capacity of the regenerated activated carbon on the organic gas with lower concentration is not strong, and the requirement of the emission standard limit value of the current purified gas is difficult to meet. The standard flow rate Q of the accumulated gas after adsorption treatment of the adsorber is determinedaCumulative purge required for desorptionGas standard flow rate QdThe ratio of (A) to (B) is defined as the concentration ratio, the larger the concentration ratio is, the better the performance of adsorption concentration is, when Q isdGreater than or equal to QaWhen the concentration ratio is 1 or less, the system loses the concentration function.
From the safety perspective, the prior method is to change the adsorbent in the concentration stage into a hydrophobic zeolite molecular sieve rotating wheel, because the zeolite molecular sieve has no flammability, even if smoldering occurs, the hazard is less than that of burning of a carbon bed, so the facility better solves the concentration problem of low-concentration and high-air-volume gas, but the investment of equipment is large, the processing and manufacturing procedures are long, the technical requirement is high, the quantity of suppliers in the world is very limited, the supply period is long, the concentration of the zeolite rotating wheel is mainly suitable for the continuous operation working condition, high-temperature air (above 160 ℃, usually 180 ℃ to 220 ℃) is required for sweeping and desorption, the requirement for desorption heat source is high, high-temperature gas is often required to be generated by burning, the application in some fireproof areas is limited, and simultaneously, because the total capacity of the zeolite molecular sieve is relatively small, the non-continuous zeolite molecular sieve is changed into a hydrophobic zeolite molecular sieve rotating wheel, Especially, the purification adaptability of organic gases with large concentration fluctuation range is not good.
Disclosure of Invention
Aiming at the problems in the prior art, the invention provides a level difference adsorption safety concentration method adopting various active carbon with wide sources, which is designed into a combined system of a main adsorber and an auxiliary adsorber by utilizing the characteristic of adsorption balance, and the main adsorber can be fully regenerated on the premise of ensuring safety through the supporting action of the level difference adsorption concentration and the auxiliary adsorber, thereby ensuring the adsorption purification efficiency of the regenerated main adsorber on low-concentration polluted gas.
Therefore, the invention adopts the following technical scheme:
an active carbon grade difference adsorption safe concentration method adopts an adsorption device which utilizes active carbon to carry out adsorption and comprises a main adsorber and an auxiliary adsorber; the safety of the main absorber during desorption is improved by the protective desorption of nitrogen inert gas (nitrogen for short), and meanwhile, the regeneration effect of activated carbon is improved by improving the temperature of the nitrogen of the main absorber, and the residual capacity of the adsorption material after desorption is reduced; after the desorbed high-concentration organic gas is properly cooled, the high-concentration organic gas is adsorbed and purified by the auxiliary adsorber to form low-concentration purge gas which is continuously used for desorption of the main adsorber, so that the desorption work of the main adsorber is completed; the auxiliary adsorber for adsorbing high-concentration gas can be regenerated by purging with air at a lower temperature, and the working capacity is recovered.
Preferably, a plurality of valves, a first gas heater, a first gas cooler and a first fan are arranged on two sides of the main adsorber; a plurality of valves, a second gas heater, a second gas cooler and a second fan are arranged on two sides of the auxiliary adsorber; the first fan is positioned between the first gas heater and the pipeline connecting point of the first gas cooler and the outlet of the gas-gas heat exchanger; the second fan is positioned on one side of an upstream gas pipeline of the second gas heater; one end of each channel of the gas-gas heat exchanger is connected with a connecting pipe between the main adsorber and the first gas cooler in a tee way, and the other end of each channel is connected with the second cooler; one end of the two ends of the other channel of the gas-gas heat exchanger is connected with the auxiliary adsorber, and the other end of the two ends of the other channel of the gas-gas heat exchanger is connected with a connecting pipe between the first fan and the first gas cooler in a tee joint manner; the valves on the left side of the main adsorber comprise a first valve, a second valve, a ninth valve and a tenth valve, and the valves on the right side comprise a third valve, a fourth valve and an eleventh valve; the valves on one side of the auxiliary adsorber comprise a fifth valve and an eighth valve, and the valves on the other side of the auxiliary adsorber comprise a sixth valve, a seventh valve and an eleventh valve; the tenth valve is used for controlling the input of nitrogen, and the eleventh valve is positioned between the main adsorber and the auxiliary adsorber; the second valve is positioned between the gas-gas heat exchanger and the main adsorber, the third valve is positioned between the first gas heater and the main adsorber, and the ninth valve is positioned between the first gas cooler and the gas-gas heat exchanger; the fifth valve is positioned between the second gas cooler and the auxiliary adsorber, and the sixth valve is positioned between the gas-gas heat exchanger and the auxiliary adsorber; a seventh valve is located between the second gas heater and the auxiliary adsorber.
Preferably, during normal adsorption operation, the first valve and the fourth valve are opened, and the second valve, the third valve, the tenth valve and the eleventh valve are closed, so as to perform adsorption purification on the gas of the main adsorber.
Further, the nitrogen replacement process before desorption of the main adsorber comprises the following steps: and closing the first valve, the second valve, the third valve, the fourth valve, the fifth valve, the sixth valve and the seventh valve, and opening the eighth valve, the eleventh valve and the tenth valve in sequence for nitrogen replacement.
Preferably, after the nitrogen purging and replacement of the main adsorber are completed, the first valve, the fourth valve, the seventh valve, the eighth valve and the ninth valve are closed, the second valve, the third valve, the fifth valve and the sixth valve are opened, and a nitrogen circulation loop including the second gas cooler, the gas-gas heat exchanger, the first fan and the first gas heater is formed by combination, wherein the operation sequence of each device is as follows: the purge gas leaving the main adsorber flows through a hot fluid inlet of the gas-gas heat exchanger through a second valve to a hot fluid outlet to be primarily cooled, then is further cooled through a second cooler and then enters the auxiliary adsorber to be subjected to adsorption purification, the purge gas obtained after purification passes through an inlet of cold side air of the gas-gas heat exchanger to an outlet to be heated, the purge gas is pressurized by a first fan, is heated to a desorption temperature through a first gas heater and then returns to the main adsorber to be subjected to purge desorption, and pollutants in the main adsorber are transferred to the auxiliary adsorber after the circulation for a certain time.
Preferably, the cooling of the main adsorber is effected by: and closing the first valve, the fourth valve, the fifth valve, the sixth valve, the tenth valve and the eleventh valve, closing the heating function of the first heater, opening the second valve, the third valve and the ninth valve, and opening the first gas cooler and the first fan for circulating cooling.
Preferably, the fifth valve, the sixth valve and the eleventh valve are closed, the eighth valve and the seventh valve are opened, the auxiliary adsorber is subjected to temperature programmed desorption by hot air generated by the second fan and the second gas heater at a temperature of less than 100 ℃, and the generated low-air-volume high-concentration gas is subjected to subsequent high-temperature thermal oxidation or recovery and other treatments.
Preferably, the auxiliary adsorber is used for receiving the high-concentration gas formed in the desorption process of the main adsorber, and the filling amount of the adsorbent in the auxiliary adsorber is 10-200% of the filling amount of the adsorbent in the main adsorber.
Preferably, the main desorption adopts high-temperature nitrogen protection circulation to fully regenerate the main adsorber with lower equilibrium adsorption capacity to form high-concentration desorption gas; after cooling to below 80 ℃, carrying out high-capacity adsorption under high equilibrium concentration by using an auxiliary adsorber, wherein the desorption temperature of a main adsorber is 100-200 ℃; the air volume of the circulating gas is 10 to 200 percent of the air volume of the main adsorber under the designed adsorption working condition.
Preferably, for the auxiliary adsorber which adsorbs pollutants with large capacity under high equilibrium concentration, hot air with the temperature lower than 100 ℃ is adopted for carrying out adsorption capacity recovery of the auxiliary adsorber; the direction of the thermal desorption gas flow of the auxiliary adsorber is opposite to the direction when the auxiliary adsorber adsorbs high-concentration gas.
Compared with the prior art, the invention has the beneficial effects that:
(1) compared with the prior active carbon adsorption concentration hot air desorption device, the invention can realize the high-efficiency adsorption of the main adsorption device under the condition of ensuring safety, thereby ensuring the adsorption and purification efficiency of the regenerated main adsorber and ensuring that the purified exhaust concentration meets the strict emission standard limit value requirement.
(2) Compared with a zeolite rotating wheel concentration device, the invention can reduce the investment cost, does not need complex zeolite modification, loading and forming processes, shortens the production supply period, and is more suitable for purification and concentration of organic gas emission in intermittent occasions with large concentration fluctuation range than a zeolite rotating wheel system.
Drawings
FIG. 1 is a schematic structural diagram of an activated carbon level difference adsorption device used in the present invention.
Description of reference numerals: 1. a first valve; 2. a second valve; 3. a third valve; 4. a fourth valve; 5. a primary adsorber; 6. an auxiliary adsorber; 7. a gas-gas heat exchanger; 8. a second gas cooler; 9. a first gas heater; 10. a second gas heater; 11. a first gas cooler; 12. a first fan; 13. a fifth valve; 14. a sixth valve; 15. a seventh valve; 16. an eighth valve; 17. a ninth valve; 18. a tenth valve; 19. an eleventh valve; 20. and a second fan.
Detailed Description
The present invention will be described in detail with reference to the accompanying drawings and specific embodiments, which are provided for illustration only and are not to be construed as limiting the invention.
The invention discloses a safe concentration method of activated carbon level difference adsorption.A adopted adsorption device utilizes activated carbon to carry out adsorption and comprises a main adsorber 5 and an auxiliary adsorber 6; the safety of the main absorber 5 during desorption is improved by nitrogen inert gas protection desorption, and meanwhile, the regeneration effect of the activated carbon is improved by improving the temperature of the nitrogen inert gas of the main absorber 5, and the residual capacity of the adsorption material after desorption is reduced; after the desorbed high-concentration organic gas is properly cooled, the high-concentration organic gas is adsorbed and purified by the auxiliary adsorber 6 to form low-concentration purging nitrogen which is continuously used for desorption of the main adsorber 5, so that the desorption work of the main adsorber is completed; the auxiliary adsorber for adsorbing high-concentration gas can be regenerated by purging with air at a lower temperature, and the working capacity is recovered.
Specifically, as shown in fig. 1, two sides of the primary adsorber 5 are provided with a plurality of valves, a first gas heater 9, a first gas cooler 11 and a first fan 12; a plurality of valves, a second gas heater 10, a second gas cooler 8 and a second fan 20 are arranged on two sides of the auxiliary absorber 6; the first fan 12 is positioned between the first gas heater 9 and the pipe connection point of the first gas cooler 11 and the outlet of the gas-gas heat exchanger 7; the second fan 20 is positioned at one side of the upstream gas pipeline of the second gas heater 10; one end of each channel of the gas-gas heat exchanger 7 is connected with a connecting pipe between the main absorber 5 and the first gas cooler in a tee way, and the other end of each channel is connected with the second cooler 8; one end of the two ends of the other channel of the gas-gas heat exchanger 7 is connected with the auxiliary adsorber 6, and the other end of the two ends of the other channel is connected with a connecting pipe between the first fan 12 and the first gas cooler 11 through a tee joint; the valves on the left side of the main adsorber 5 comprise a first valve 1, a second valve 2, a ninth valve 17 and a tenth valve 18, and the valves on the right side comprise a third valve 3, a fourth valve 4 and an eleventh valve 19; the valves on one side of the auxiliary adsorber 6 comprise a fifth valve 13 and an eighth valve 16, and the valves on the other side comprise a sixth valve 14, a seventh valve 15 and an eleventh valve 19; a tenth valve 18 for controlling the nitrogen input, an eleventh valve 19 being located between the primary adsorber 5 and the auxiliary adsorber 6; the second valve 2 is located between the gas-gas heat exchanger 7 and the primary adsorber 5, the third valve 3 is located between the first gas heater 9 and the primary adsorber 5, and the ninth valve 17 is located between the first gas cooler 11 and the gas-gas heat exchanger 7; a fifth valve 13 is located between the second gas cooler 8 and the auxiliary adsorber 6, and a sixth valve 14 is located between the gas-gas heat exchanger 7 and the auxiliary adsorber 6; a seventh valve 15 is located between the second gas heater 10 and the auxiliary adsorber 6.
Specifically, in normal adsorption operation, the first valve 1 and the fourth valve 4 are opened, and the second valve 2, the third valve 3, the tenth valve 18, and the eleventh valve 19 are closed, so that the main adsorber 5 is purged by gas adsorption.
Specifically, the nitrogen replacement process before desorption of the main adsorber comprises the following steps: the first valve 1, the second valve 2, the third valve 3, the fourth valve 4, the fifth valve 13, the sixth valve 14 and the seventh valve 15 are closed, and the eighth valve 16, the eleventh valve 19 and the tenth valve 18 are sequentially opened to perform nitrogen substitution.
Specifically, the main adsorber after nitrogen replacement is completed is combined to form a nitrogen circulation loop including the second gas cooler 8, the gas-gas heat exchanger 7, the first fan 12 and the first gas heater 9 by closing the first valve 1, the fourth valve 4, the seventh valve 15, the eighth valve 16 and the ninth valve 17 and opening the second valve 2, the third valve 3, the fifth valve 13 and the sixth valve 14, and the operation sequence of each device is as follows: the purge gas leaving the primary adsorber 5 flows through the hot fluid inlet of the gas-gas heat exchanger 7 to the hot fluid outlet through the second valve 2 to be primarily cooled, then further cooled by the second cooler 8 and enters the secondary adsorber 6 to be adsorbed and purified, the obtained purified purge gas is heated through the cold side air inlet of the gas-gas heat exchanger 7 to the outlet, is pressurized by the first fan 12, is heated to the desorption temperature by the first gas heater 9, and then returns to the primary adsorber 5 to be subjected to hot gas purging desorption, and pollutants in the primary adsorber 5 are transferred to the secondary adsorber 6 after the cycle is performed for a certain time.
In particular, the cooling of the main adsorber 5 is achieved by: the first valve 1, the fourth valve 4, the fifth valve 13, the sixth valve 14, the tenth valve 18, and the eleventh valve 19 are closed, the heating function of the first heater 9 is closed, the second valve 2, the third valve 3, and the ninth valve 17 are opened, and the first gas cooler 11 and the first fan 12 are opened to perform the circulation cooling.
Specifically, the fifth valve 13, the sixth valve 14, and the eleventh valve 19 are closed, the eighth valve 16 and the seventh valve 15 are opened, the auxiliary adsorber 6 is subjected to temperature programmed desorption at 100 ℃ or lower by hot air generated by the second fan 20 and the second gas heater 10, and the generated low-air-volume high-concentration gas is subjected to subsequent high-temperature thermal oxidation or the like.
Specifically, the auxiliary adsorber 6 is adopted to receive the high-concentration gas formed in the desorption process of the main adsorber 5, and the filling amount of the adsorbent in the auxiliary adsorber 6 is 10-200% of the filling amount of the adsorbent in the main adsorber 5.
Specifically, the main desorption adopts high-temperature nitrogen protection circulation to fully regenerate the main adsorber 5 with lower equilibrium adsorption capacity to form high-concentration desorption gas; after cooling to below 80 ℃, carrying out high-capacity adsorption under high equilibrium concentration by using an auxiliary adsorber 6, wherein the desorption temperature of a main adsorber 5 is 100-200 ℃; the air volume of the circulating gas is 10 to 200 percent of the air volume of the main adsorber under the designed adsorption working condition.
Specifically, for the auxiliary adsorber 6 which adsorbs pollutants in large capacity under high equilibrium concentration, hot air with the temperature lower than 100 ℃ is adopted for carrying out adsorption capacity recovery of the auxiliary adsorber; the direction of the thermal desorption gas flow of the auxiliary adsorber 6 is opposite to the direction when it adsorbs the high concentration gas.
The step adsorption concentration is that the adsorption balance characteristic is utilized to design a combined system of a main adsorber and an auxiliary adsorber, nitrogen inert gas is adopted to protect the high-temperature desorption main adsorber, the desorbed high-concentration gas is properly cooled and then is adsorbed again by the auxiliary adsorber, and finally the temperature programmed desorption of the temperature below 100 ℃ is carried out on the auxiliary adsorber adsorbing the high-concentration gas by adopting air. The adsorbent has the characteristics of low adsorption capacity at low concentration and high temperature and high adsorption capacity at low temperature and high concentration, so that the main adsorber can be fully regenerated on the premise of ensuring safety through the adsorption concentration of the above grade difference and the supporting action of the auxiliary adsorber, thereby ensuring the adsorption purification efficiency of the regenerated main adsorber.
The above description is only exemplary of the present invention and should not be taken as limiting the invention, as any modification, equivalent replacement, or improvement made within the spirit and scope of the present invention should be included in the present invention.
Claims (9)
1. The utility model provides an active carbon level difference adsorbs safe concentration method, the adsorption equipment who adopts utilizes active carbon to adsorb, includes main adsorber (5) and supplementary adsorber (6), its characterized in that: the safety of the main absorber (5) during desorption is improved through nitrogen inert gas protection desorption, and meanwhile, the regeneration effect of the activated carbon is improved through improving the temperature of the nitrogen inert gas of the main absorber (5), and the residual capacity of the adsorption material after desorption is reduced; after being properly cooled, the desorbed high-concentration organic gas is adsorbed and purified by the auxiliary adsorber (6) to form low-concentration purge gas which is continuously used for desorption of the main adsorber (5), so that the desorption work of the main adsorber is completed; an auxiliary adsorber for adsorbing high-concentration gas is purged by air at a lower regeneration temperature, and the working capacity is recovered by regeneration;
a plurality of valves, a first gas heater (9), a first gas cooler (11) and a first fan (12) are arranged on two sides of the main absorber (5); a plurality of valves, a second gas heater (10), a second gas cooler (8) and a second fan (20) are arranged on two sides of the auxiliary absorber (6); the first fan (12) is positioned between the first gas heater (9) and the pipeline connecting point of the first gas cooler (11) and the outlet of the gas-gas heat exchanger (7); the second fan (20) is positioned on one side of an upstream gas pipeline of the second gas heater (10); one end of each channel of the gas-gas heat exchanger (7) is connected with a connecting pipe between the main absorber (5) and the first gas cooler in a tee way, and the other end of each channel is connected with the second gas cooler (8); one end of the two ends of the other channel of the gas-gas heat exchanger (7) is connected with the auxiliary adsorber (6), and the other end of the two channels is connected with a connecting pipe between the first fan (12) and the first gas cooler (11) in a tee joint manner; the valves on the left side of the main adsorber (5) comprise a first valve (1), a second valve (2), a ninth valve (17) and a tenth valve (18), and the valves on the right side comprise a third valve (3), a fourth valve (4) and an eleventh valve (19); the valves on one side of the auxiliary adsorber (6) comprise a fifth valve (13) and an eighth valve (16), and the valves on the other side comprise a sixth valve (14), a seventh valve (15) and an eleventh valve (19); a tenth valve (18) for controlling the nitrogen input, an eleventh valve (19) being located between the primary adsorber (5) and the auxiliary adsorber (6); the second valve (2) is located between the gas-gas heat exchanger (7) and the main adsorber (5), the third valve (3) is located between the first gas heater (9) and the main adsorber (5), and the ninth valve (17) is located between the first gas cooler (11) and the gas-gas heat exchanger (7); a fifth valve (13) is located between the second gas cooler (8) and the auxiliary adsorber (6), and a sixth valve (14) is located between the gas-gas heat exchanger (7) and the auxiliary adsorber (6); the seventh valve (15) is located between the second gas heater (10) and the auxiliary adsorber (6).
2. The activated carbon level difference adsorption safety concentration method according to claim 1, characterized in that: and in normal adsorption operation, the first valve (1) and the fourth valve (4) are opened, the second valve (2), the third valve (3), the tenth valve (18) and the eleventh valve (19) are closed, and the gas adsorption and purification of the main adsorber (5) are carried out.
3. The activated carbon level difference adsorption safety concentration method according to claim 1, characterized in that: the nitrogen replacement process before desorption of the main adsorber comprises the following steps: and closing the first valve (1), the second valve (2), the third valve (3), the fourth valve (4), the fifth valve (13), the sixth valve (14) and the seventh valve (15), and sequentially opening the eighth valve (16), the eleventh valve (19) and the tenth valve (18) for nitrogen replacement.
4. The activated carbon level difference adsorption safety concentration method according to claim 1, characterized in that: after the nitrogen purging and replacement of the main adsorber are completed, the second valve (2), the third valve (3), the fifth valve (13) and the sixth valve (14) are opened by closing the first valve (1), the fourth valve (4), the seventh valve (15), the eighth valve (16) and the ninth valve (17), so that a nitrogen circulation loop comprising the second gas cooler (8), the gas-gas heat exchanger (7), the first fan (12) and the first gas heater (9) is formed in a combined manner, and the action sequence of each device is as follows: the purging desorption gas leaving the main adsorber (5) flows through a hot fluid inlet of the gas-gas heat exchanger (7) to a hot fluid outlet through a second valve (2) to be initially cooled, then is further cooled through a second gas cooler (8) and then enters the auxiliary adsorber (6) to be adsorbed and purified, the obtained purified purging gas is heated from an inlet to an outlet of cold side air of the gas-gas heat exchanger (7), is heated to the desorption temperature through a first gas heater (9) after being pressurized by a first fan (12), returns to the main adsorber (5) to be subjected to hot gas purging desorption, and pollutants in the main adsorber (5) are transferred to the auxiliary adsorber (6) after the circulation for a certain time.
5. The activated carbon level difference adsorption safety concentration method according to claim 1, characterized in that: the cooling of the main adsorber (5) is effected by: the first valve (1), the fourth valve (4), the fifth valve (13), the sixth valve (14), the tenth valve (18) and the eleventh valve (19) are closed, the heating function of the first gas heater (9) is closed, the second valve (2), the third valve (3) and the ninth valve (17) are opened, and the first gas cooler (11) and the first fan (12) are opened to carry out circulating cooling.
6. The activated carbon level difference adsorption safety concentration method according to claim 1, characterized in that: and closing the fifth valve (13), the sixth valve (14) and the eleventh valve (19), opening the eighth valve (16) and the seventh valve (15), performing temperature programmed desorption on the auxiliary adsorber (6) at the temperature of below 100 ℃ by using hot air generated by the second fan (20) and the second gas heater (10), and performing subsequent treatment systems such as high-temperature thermal oxidation or recovery on the generated low-air-volume high-concentration gas.
7. The activated carbon level difference adsorption safety concentration method according to any one of claims 1 to 6, characterized in that: the auxiliary adsorber (6) is adopted to receive the high-concentration gas formed in the desorption process of the main adsorber (5), and the filling amount of the adsorbent in the auxiliary adsorber (6) is 10-200% of the filling amount of the adsorbent in the main adsorber (5).
8. The activated carbon level difference adsorption safety concentration method according to claim 7, characterized in that: the main desorption adopts high-temperature nitrogen protection circulation to fully regenerate the main adsorber (5) with lower equilibrium adsorption capacity to form high-concentration desorption gas; after cooling to below 80 ℃, carrying out high-capacity adsorption under high equilibrium concentration by using an auxiliary adsorber (6), wherein the desorption temperature of a main adsorber (5) is 100-200 ℃; the air volume of the circulating gas is 10 to 200 percent of the air volume of the main adsorber under the designed adsorption working condition.
9. The activated carbon level difference adsorption safety concentration method according to claim 8, characterized in that: for the auxiliary adsorber (6) which adsorbs pollutants with large capacity under high equilibrium concentration, the adsorption capacity of the auxiliary adsorber is recovered by adopting hot air with the temperature lower than 100 ℃; the direction of the thermal desorption gas flow of the auxiliary adsorber (6) is opposite to the direction when the auxiliary adsorber adsorbs the high-concentration gas.
Priority Applications (1)
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