CN116550086A - Adsorption and water vapor desorption condensation recovery process and device - Google Patents
Adsorption and water vapor desorption condensation recovery process and device Download PDFInfo
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- CN116550086A CN116550086A CN202310048501.6A CN202310048501A CN116550086A CN 116550086 A CN116550086 A CN 116550086A CN 202310048501 A CN202310048501 A CN 202310048501A CN 116550086 A CN116550086 A CN 116550086A
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- 238000001179 sorption measurement Methods 0.000 title claims abstract description 400
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 135
- 238000003795 desorption Methods 0.000 title claims abstract description 99
- 238000009833 condensation Methods 0.000 title claims abstract description 29
- 230000005494 condensation Effects 0.000 title claims abstract description 29
- 238000011084 recovery Methods 0.000 title claims abstract description 20
- 238000001816 cooling Methods 0.000 claims abstract description 179
- 238000001035 drying Methods 0.000 claims abstract description 168
- 239000007789 gas Substances 0.000 claims abstract description 92
- 239000003463 adsorbent Substances 0.000 claims abstract description 76
- 239000002904 solvent Substances 0.000 claims abstract description 37
- 239000010815 organic waste Substances 0.000 claims abstract description 34
- 239000002912 waste gas Substances 0.000 claims abstract description 11
- 239000007788 liquid Substances 0.000 claims description 74
- 238000007599 discharging Methods 0.000 claims description 38
- 238000007789 sealing Methods 0.000 claims description 37
- 238000000034 method Methods 0.000 claims description 21
- 230000008569 process Effects 0.000 claims description 16
- 230000001105 regulatory effect Effects 0.000 claims description 15
- 238000010926 purge Methods 0.000 claims description 14
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 12
- 230000007613 environmental effect Effects 0.000 claims description 11
- 229910002804 graphite Inorganic materials 0.000 claims description 6
- 239000010439 graphite Substances 0.000 claims description 6
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- 238000010408 sweeping Methods 0.000 claims description 6
- 239000005416 organic matter Substances 0.000 claims description 5
- 238000007664 blowing Methods 0.000 claims description 4
- 238000009835 boiling Methods 0.000 claims description 2
- 230000009467 reduction Effects 0.000 claims description 2
- 239000011347 resin Substances 0.000 claims description 2
- 229920005989 resin Polymers 0.000 claims description 2
- 125000004122 cyclic group Chemical group 0.000 claims 2
- 229920006395 saturated elastomer Polymers 0.000 claims 2
- 229920000049 Carbon (fiber) Polymers 0.000 claims 1
- 238000011946 reduction process Methods 0.000 claims 1
- 239000012855 volatile organic compound Substances 0.000 abstract description 10
- 238000005516 engineering process Methods 0.000 description 5
- 238000010586 diagram Methods 0.000 description 4
- 239000011259 mixed solution Substances 0.000 description 4
- 230000006837 decompression Effects 0.000 description 3
- 239000000443 aerosol Substances 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 238000005507 spraying Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 1
- 206010037544 Purging Diseases 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000007084 catalytic combustion reaction Methods 0.000 description 1
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- 238000002485 combustion reaction Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 239000002360 explosive Substances 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical class C VNWKTOKETHGBQD-UHFFFAOYSA-N 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
- B01D53/04—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 with stationary adsorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0003—Condensation of vapours; Recovering volatile solvents by condensation by using heat-exchange surfaces for indirect contact between gases or vapours and the cooling medium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0033—Other features
- B01D5/0036—Multiple-effect condensation; Fractional condensation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0033—Other features
- B01D5/0054—General arrangements, e.g. flow sheets
-
- 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
- B01D53/04—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 with stationary adsorbents
- B01D53/0407—Constructional details of adsorbing systems
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/10—Inorganic adsorbents
- B01D2253/102—Carbon
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/20—Organic adsorbents
- B01D2253/202—Polymeric adsorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
- B01D2257/708—Volatile organic compounds V.O.C.'s
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/40083—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption
- B01D2259/40088—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating
- B01D2259/4009—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating using hot gas
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
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- Oil, Petroleum & Natural Gas (AREA)
- Treating Waste Gases (AREA)
- Separation Of Gases By Adsorption (AREA)
Abstract
The invention relates to the technical field of organic waste gas treatment and discloses an adsorption and water vapor desorption condensation recovery process and a device, wherein the adsorption and water vapor desorption condensation recovery process comprises an induced draft fan, an adsorption tank, a vapor buffer tank, a condenser, an adsorption tank condensation water cooler, a drying cooling fan, a drying cooling air heat exchanger, a solvent collection tank and a solvent delivery pump; the number of the adsorption tanks is n+1 (n is an integer greater than or equal to 1), and during normal operation, the adsorption tanks can be connected with the adsorption tanks in series for desorbing and drying and cooling 1, and the adsorption tanks can be connected with the adsorption tanks in parallel for desorbing and drying and cooling 1. The invention solves the problems of high pressure of the existing desorption steam, uncontrollable desorption temperature, short-time discharge exceeding standard when the adsorbent is dried and cooled, and the like, and can efficiently remove volatile organic compounds in the waste gas.
Description
Technical Field
The invention relates to an adsorption and water vapor desorption condensation recovery process and device, which are applied to an organic waste gas treatment system and belong to the technical field of organic waste gas treatment.
Background
In the industrial production process, a large amount of Volatile Organic Compounds (VOCs) are discharged, so that the air quality is seriously influenced, the volatile organic compounds are not only primary pollution sources, but also secondary pollution of optical smog and the like can be caused, and certain organic compounds can form organic aerosol through the processes of nucleation, condensation, gas particle distribution and the like due to lower vapor pressure, and the organic aerosol is an important component of PM 2.5; secondly, volatile organic compounds are harmful to human health and have direct toxic action on human bodies; part of volatile organic compounds can destroy an ozone layer, bring more extensive influence to organisms, and most of volatile organic compounds belong to inflammable and explosive objects, and are easy to explode when discharged in high concentration. Therefore, the national emphasis on preventing and treating VOCs is that of environmental protection, and at present, several main VOCs treatment technologies are as follows: adsorption techniques, absorption techniques, combustion methods (including direct combustion and catalytic combustion), combination techniques (techniques that combine various abatement processes using the characteristics of the organic exhaust gas), and the like. The most commonly used technology at present is the adsorption and water vapor desorption condensation recovery technology, which is suitable for the treatment of most organic waste gases, but has the following problems: the invention provides a novel adsorption and water vapor condensation recovery process for solving the problems, which is characterized in that (1) because middle-low pressure water vapor is adopted (the water vapor pressure is more than or equal to 0.1MPa (the pressure is gauge pressure, the pressure which is not specially described later is gauge pressure), the design pressure of an adsorption tank is more than or equal to 0.1MPa, the adsorption tank is designed and manufactured according to the requirement of the pressure tank, (2) because the temperature of the water vapor is high, the temperature of the water vapor can possibly cause the original organic matters to be converted from a physical adsorption state to a chemical adsorption state, so that the bond energy of an adsorption bond is greatly increased, and the desorption is difficult to come down, and (3) after the desorption of the adsorption tank is completed, air is directly introduced to purge and dry the adsorption tank, and the high-concentration organic matters are directly introduced into a chimney in the initial stage of purging, so that the emission exceeds the standard.
Disclosure of Invention
In order to solve the problems that the pressure of the existing desorption steam is too high, the desorption temperature cannot be controlled, short-time emission exceeds standard when the adsorbent is dried and cooled, and the like, the invention designs a more scientific and reasonable adsorption and steam desorption condensation recovery process, which can efficiently remove volatile organic compounds in waste gas, and simultaneously adopts steam lower than 0.1MPa for desorption, thereby realizing the purpose that the adsorption tank is a non-pressure container; meanwhile, as lower steam is adopted for desorption, an automatic valve is not required to be arranged on a condensate discharging pipeline at the bottom of the adsorption tank and a condensate discharging pipeline of the condenser, and the sealing of the condensate discharging pipeline of the adsorption tank and the condensate discharging pipeline of the condenser can be realized through liquid sealing, so that the system flow is simplified, the reliability and the safety of the operation of the device are improved, and the workload of operation and maintenance is reduced; meanwhile, the temperature of the water vapor is controlled by adopting a water spraying temperature control technology, so that the aim that the desorption temperature is more beneficial to desorbing organic matters from the adsorbent is fulfilled; meanwhile, the method of combining closed drying cooling and open drying cooling is adopted, so that the aim that the exhaust emission reaches the standard in the drying and cooling process of the adsorbent is fulfilled.
In order to achieve the above object, the present invention is achieved by the following technical solutions.
The adsorption and water vapor desorption condensation recovery process comprises an induced draft fan, an adsorption tank, a vapor buffer tank, a condenser, an adsorption tank condensation water cooler, a drying cooling fan, a drying cooling air heat exchanger, a solvent collection tank and a solvent delivery pump.
The number of the adsorption tanks is n+1 (n is an integer greater than or equal to 1), and during normal operation, the adsorption operation is carried out on the n adsorption tanks, and the desorption operation is carried out on the 1 adsorption tank.
Further, n adsorption tanks are connected in series for adsorption, the organic waste gas is pressurized by an induced draft fan and sequentially enters n adsorption tanks (n adsorption tanks are connected in series), when the organic waste gas passes through the adsorption tanks, the organic matters in the waste gas are adsorbed by the adsorbent in the adsorption tanks, and when the organic waste gas is discharged from the last adsorption tank, the concentration of the organic matters in the waste gas meets the environmental protection discharge requirement and is sent to an exhaust funnel for high-altitude discharge.
Or, the n adsorption tanks are connected in parallel for adsorption, the organic waste gas enters the n adsorption tanks (the n adsorption tanks are connected in parallel) after being pressurized by the induced draft fan, when the organic waste gas passes through the adsorption tanks, the organic matters in the waste gas are adsorbed by the adsorbent in the adsorption tanks, and when the organic waste gas is discharged from the adsorption tanks, the concentration of the organic matters in the waste gas meets the environmental protection discharge requirement and is sent to an exhaust funnel for high-altitude discharge.
Further, the adsorbent in the adsorption tank is columnar granular activated carbon, macroporous resin, activated carbon fiber and the like.
Further, the adsorption tank is of a horizontal double-oval end socket, or a vertical flat top cone bottom structure.
The adsorption tank needs to carry out desorption operation after adsorption saturation, desorption steam is depressurized to be below 0.1MPa and enters the steam buffer tank, at the moment, the steam is superheated steam, the superheated steam enters the adsorption tank needing to be desorbed after water spray temperature reduction, under the blowing of the water steam, organic matters are desorbed from the inside of the adsorbent, the organic matters steam containing water steam enters the condenser from the adsorption tank, the organic matters steam containing water steam is converted into liquid from gas state and is collected in the solvent collection tank.
Furthermore, the design pressure of the adsorption tank is less than 0.1MPa, and the adsorption tank is a non-pressure container.
Further, the pressure of the steam is reduced to below 0.1MPa through one-stage or two-stage decompression, a decompression valve can be adopted in a decompression mode, a self-standing pressure regulating valve can be adopted, or a regulating valve can be adopted.
Further, the temperature of the desorption steam is regulated through a water spraying and temperature reducing process, namely, the temperature of the water steam is controlled through regulating the quantity of the sprayed water, and a water inlet valve is a regulating valve or an automatic switching valve.
Furthermore, the condenser is in a single-stage or double-stage mode, the condensation stage number is determined according to the boiling point of condensed organic matters, and the type of the condenser is a vertical or horizontal shell-and-tube heat exchanger, and also can be a vertical or horizontal graphite heat exchanger.
Further, after the water vapor enters the adsorption tank, part of the water vapor is directly condensed into liquid, the liquid is collected at the bottom of the adsorption tank, flows to a condensation water cooler of the adsorption tank through a liquid drain pipe at the bottom of the adsorption tank, the liquid cooled by the heat exchanger is collected in a solvent collecting tank, and the condensation water cooler of the adsorption tank is a spiral plate type heat exchanger or a graphite heat exchanger.
Furthermore, the condensate water drainage pipeline at the bottom of the adsorption tank is not provided with a valve, each condensate water drainage pipeline at the bottom of the adsorption tank is provided with a liquid seal pipe, the liquid seal height is at least 500mm, and the sealing of the condensate water drainage pipeline at the bottom of the adsorption tank can be realized through the liquid seal due to the low working pressure of the adsorption tank.
Furthermore, the condensate outlet pipeline at the bottom of the condenser is not provided with a valve, a section of liquid seal pipe is arranged, the height of the liquid seal is at least 500mm, and the sealing of the condensate outlet pipeline of the condenser can be realized through the liquid seal due to the low working pressure of the condenser.
After the desorption of the adsorption tank is completed, the adsorbent in the adsorption tank is required to be cooled and dried, and closed cooling and drying are adopted in the initial stage: starting a drying cooling fan to purge heat and water vapor contained in the adsorbent in the adsorption tank, and simultaneously taking out organic waste gas in the adsorption tank, wherein the purged gas enters a drying cooling air heat exchanger, the water vapor in the gas phase is condensed into water after the gas is subjected to heat exchange cooling, the cooled and dehydrated gas returns to an inlet of the drying cooling fan and is blown into the adsorption tank again to dry and cool the adsorbent again, after a period of circulating drying cooling, the temperature of the adsorbent in the adsorption tank is reduced, and the organic matters in the drying cooling air are also re-adsorbed by the adsorbent, so that closed cooling drying is switched into open cooling drying: opening an inlet valve of a drying cooling fan, directly extracting air from the atmosphere by the drying cooling fan, drying and cooling the adsorbent in the adsorption tank, and directly discharging the high-temperature gas containing water vapor into an exhaust barrel by blowing.
Further, the drying cooling air heat exchanger is a tube fin type heat exchanger or a graphite heat exchanger.
Further, the dry cooling air inlet valve is an automatic valve or a check valve.
Further, after the vapor is condensed into liquid water in the drying and cooling air heat exchanger, the liquid water is discharged through a clean discharge pipeline at the bottom of the heat exchanger, a valve is not arranged on the clean discharge pipeline, a section of liquid seal pipe is arranged, the liquid seal height is at least 500mm, and the sealing of the clean discharge pipeline of the drying and cooling air heat exchanger can be realized through the liquid seal due to lower working pressure of the drying and cooling air heat exchanger.
And condensed water at the bottom of the adsorption tank, condensed water discharged from the condenser and condensed water discharged from the drying cooling air heat exchanger are collected and discharged into the solvent collecting tank, and are sent out through the solvent conveying pump.
Furthermore, the top emptying pipeline of the solvent collecting tank is connected to the organic waste gas inlet main pipe of the adsorption and water vapor desorption condensation recovery device, so that direct emptying is avoided.
The invention has the following advantages:
(1) The water vapor with pressure lower than 0.1MPa is adopted for desorption, so that the purpose that the adsorption tank is a non-pressure container is realized, the manufacturing cost of the adsorption tank is reduced, and meanwhile, the operation of the adsorption tank is safer;
(2) The lower steam is adopted for desorption, the working pressure of the system is lower, automatic valves are not arranged on a condensate discharging pipeline at the bottom of the adsorption tank and a condensate discharging pipeline at the bottom of the condenser, and the sealing of the condensate discharging pipeline of the adsorption tank and the condensate discharging pipeline of the condenser can be realized through a liquid sealing pipeline, so that the system flow is simplified, the reliability and the safety of the operation of the device are improved, and the workload of the operation and maintenance is reduced;
(3) The temperature of water vapor is controlled by adopting a water spray temperature control technology, so that the temperature during desorption can be adjusted, the organic matters are ensured to be desorbed at an optimal temperature point, and the condition that the organic matters are converted from a physical adsorption state to a chemical adsorption state due to the excessive vapor temperature is avoided, so that the bond energy of adsorption bonds is greatly increased, and the desorption is difficult to occur;
(4) The mode of combining closed drying cooling and open drying cooling is adopted, so that the problem that the exhaust emission exceeds standard in the drying and cooling process of the adsorbent is solved.
Drawings
The foregoing and other objects and advantages of the invention will be more readily and clearly understood from the following detailed description of the preferred embodiments of the invention, taken in conjunction with the accompanying drawings.
FIG. 1 is a schematic diagram of the process flow of the present invention when two adsorption tanks (one adsorption and one desorption) are provided;
FIG. 2 is a schematic diagram of a process flow in the present invention when three adsorption tanks (two adsorption and one desorption, adsorption tanks are connected in series);
FIG. 3 is a second schematic diagram of the process flow of the present invention when three adsorption tanks (two adsorption and one desorption, adsorption tanks are connected in series) are provided;
FIG. 4 is a schematic diagram of the process flow of the present invention when three adsorption tanks (two adsorption and one desorption, adsorption tanks are connected in parallel) are provided;
in the figure, 1, a draught fan, 2, a adsorption tank, 3,4, a adsorption tank, 5, a steam buffer tank, 6, a primary condenser, 7, a secondary condenser, 8, a adsorption tank condensate cooler, 9, a drying cooling fan, 10, a drying cooling air heat exchanger, 11, a solvent collecting tank, 12, a solvent delivery pump, 2-1, 2-2, 2-3, 2-4, 2-5, 2-6, 2-7, 2-8, 2-9, 3-1, 3-2, 3-3, 3-4, 3-5, 3-6, 3-7, 3-8, 3-9, 4-1, 4-2, 4-3, 4-4, 4-5, 4-6, 4-7, 4-8, 4-9, 5-9, and 5-1, and 5-9.
Description of the embodiments
The invention will be further described with reference to specific examples, but the scope of the invention is not limited thereto.
Example 1
Referring to fig. 1, the one-suction one-desorption process has two adsorption tanks in total, and one adsorption tank is in adsorption and the other adsorption tank is in desorption, drying and cooling during normal operation.
The adsorption tank 2 is adsorbed, and the desorption, drying, and cooling of the adsorption tank 3 will be described in detail.
The organic waste gas is fed into an inlet of an adsorption tank 2 after being pressurized by an induced draft fan 1, at the moment, an inlet valve 2-1 of the adsorption tank 2 is opened, an outlet valve 2-3 of the adsorption tank 2 is opened, the valves 2-2, 2-4, 2-5, 2-6 and 2-7 are all closed, the organic waste gas enters the adsorption tank 2, passes through an adsorbent layer in the adsorption tank 2, and is captured and adsorbed by the adsorbent to be removed, and purified gas is discharged from the adsorption tank 2 and enters an exhaust barrel to reach the discharge standard.
The adsorption tank 2 is subjected to adsorption operation, the adsorption tank 3 is subjected to desorption operation, water vapor is depressurized to be below 0.1MPa through a valve 5-1 and then enters a vapor buffer tank 5, at the moment, the vapor is superheated vapor, a certain amount of pure water is sprayed into the vapor buffer tank to cool the superheated vapor, the sprayed pure water flow is regulated by regulating the opening of the valve 5-3, so that the temperature of the water vapor is controlled, the vapor reaching the required temperature is conveyed to a vapor inlet of the adsorption tank 3, at the moment, a vapor inlet valve 3-5 of the adsorption tank 3 and a valve 3-7 are opened, the valve 3-1, the valve 3-2, the valve 3-3, the valve 3-4 and the valve 3-6 are all closed, the vapor enters the adsorption tank 3, a part of the water vapor is directly condensed into the adsorption tank 3 and is collected to the bottom of the adsorption tank 3, the superheated vapor is discharged through a condensate water discharging pipe at the bottom of the adsorption tank 3, the valve is not arranged on the discharging pipe, the sealing of the discharging pipe is realized through a liquid seal, the liquid seal height is more than or equal to 500mm, and the discharged condensate is discharged into a solvent collecting tank 11 after the cooling in an adsorption condensate water cooler 8; under the continuous sweeping of the water vapor, the organic matters are desorbed from the inside of the adsorbent, the organic matters vapor desorbed from the water vapor enters the first-stage condenser 6 and the second-stage condenser 7 from the adsorption tank 3, the organic matters vapor containing the water vapor is converted into liquid from gas, the liquid is discharged from the first-stage condenser 6 and the second-stage condenser 7, the mixed solution of the liquid water and the organic matters is collected into the solvent collecting tank 11, the condensate discharging pipelines of the first-stage condenser 6 and the second-stage condenser 7 are not provided with valves, the sealing of the condensate discharging pipelines of the first-stage condenser 6 and the second-stage condenser 7 is realized by setting liquid seals, and the liquid seal height is more than or equal to 500mm.
After the desorption of the adsorption tank 3 is completed, the adsorption tank is transferred to a drying and cooling operation, closed drying and cooling are firstly adopted, at the moment, the valves 3-1, 3-3, 3-5, 3-6 and 3-7 of the adsorption tank 3 are closed, the valves 3-2 and 3-4 are opened, the drying and cooling fan 9 is started, meanwhile, the inlet valve 9-1 of the drying and cooling fan 9 is closed, air is pressurized by the drying and cooling fan 9 and enters the adsorption tank 3, heat and water vapor in the adsorbent of the adsorption tank 3 are purged out, organic waste gas in the adsorption tank 3 is carried out, the purged gas enters the drying and cooling air heat exchanger 10, the water vapor in the gas phase is condensed into water after the gas is subjected to heat exchange and cooling, the water is discharged into the solvent collecting tank 11 through a purge pipeline of the drying and cooling air heat exchanger 10, the purge pipeline is not provided with a valve, a section of liquid sealing pipe is arranged, the liquid sealing height is at least 500mm, and the sealing of the purge pipeline of the drying and cooling air heat exchanger 10 is realized through liquid sealing; the cooled and dehydrated gas returns to the inlet of the drying and cooling fan 9 and is blown into the adsorption tank 3 again to dry and cool the adsorbent again, after a period of circulating drying and cooling, the temperature of the adsorbent in the adsorption tank 3 is reduced, and the organic matters in the drying and cooling air are also re-adsorbed by the adsorbent, so that closed cooling and drying are carried out into open cooling and drying: opening an inlet valve 9-1 of a drying cooling fan 9, opening a valve 3-3, closing a valve 3-4, directly extracting air from the atmosphere by the drying cooling fan 9, drying and cooling the adsorbent in the adsorption tank 3, directly discharging the high-temperature gas containing water vapor which is purged out into an exhaust barrel, and when the temperature of the adsorbent in the adsorption tank 3 is lower than 50 ℃, completing the drying and cooling operation because the organic matters in the gas in the adsorption tank 3 are re-adsorbed by the adsorbent, and the discharged gas meets the environmental protection emission requirement.
When the adsorption tank 3 is completed with desorption, drying and cooling operations, the adsorption tank 2 can be switched into desorption, drying and cooling operations, and the two adsorption tanks alternately perform adsorption, desorption and drying and cooling operations, and the adsorption tank is continuously operated in a cycle.
The liquid stored in the solvent collection tank 11 is transported outside by the solvent transport pump 12.
Example 2
Referring to fig. 2, the two adsorption and one desorption processes have three adsorption tanks in total, and in normal operation, two adsorption tanks are connected in series for adsorption (the series mode is shown as the figure), and the other adsorption tank is used for desorption, drying and cooling.
The adsorption tank 2 is first-stage adsorbed, the adsorption tank 3 is second-stage adsorbed, and the desorption, drying and cooling of the adsorption tank 4 are described in detail.
The organic waste gas is fed to an inlet of an adsorption tank 2 after being pressurized by an induced draft fan 1, at the moment, an inlet valve 2-2 of the adsorption tank 2 is opened, an outlet valve 2-5 of the adsorption tank 2 is opened, valves 2-1, 2-3, 2-4, 2-6, 2-7, 2-8 and 2-9 are all closed, an inlet valve 3-1 of the adsorption tank 3 is opened, an outlet valve 3-4 of the adsorption tank 3 is opened, the valves 3-2, 3-3, 3-5, 3-6, 3-7, 3-8 and 3-9 are all closed, the organic waste gas sequentially enters the adsorption tank 2 and 3, passes through an adsorbent layer inside the adsorption tank 2 and 3, and then the organic matter is captured and adsorbed by the adsorbent to be removed, the purified gas is discharged from the adsorption tank 3, and enters an exhaust pipe to reach the standard for emission.
The adsorption tank 2 and the adsorption tank 3 are subjected to adsorption operation, the adsorption tank 4 is subjected to desorption operation, water vapor is depressurized to be below 0.1MPa through a valve 5-1 and then enters a vapor buffer tank 5, at the moment, the vapor is superheated vapor, a certain amount of pure water is sprayed into the vapor buffer tank to cool the superheated vapor, the sprayed pure water flow is regulated by regulating the opening degree of the valve 5-3, so that the temperature of the water vapor is controlled, the vapor reaching the required temperature is conveyed to a vapor inlet of the adsorption tank 4, at the moment, a vapor inlet valve 4-7 and a valve 4-9 of the adsorption tank 4 are opened, the valve 4-1, the valve 4-2, the valve 4-3, the valve 4-4, the valve 4-5, the valve 4-6 and the valve 4-8 are all closed, the vapor enters the adsorption tank 4, a part of the vapor is directly condensed into the adsorption tank 4 to be collected to the bottom of the adsorption tank 4, the condensate water at the bottom of the adsorption tank 4 is discharged through a condensate water discharging pipe, the valve is not arranged on the discharging pipe, the sealing of the discharging pipe of the adsorption tank 4 is realized, the condensate water discharging pipe is discharged into a condensate water cooler 11 after the condensate water cooler is cooled by the condensate tank 11, and the condensate water is discharged into the condensate tank 11 after the condensate tank is cooled by the condensate tank at the height of 500 mm; under the continuous sweeping of the water vapor, the organic matters are desorbed from the inside of the adsorbent, the organic matters vapor desorbed from the water vapor enters the first-stage condenser 6 and the second-stage condenser 7 from the adsorption tank 4, the organic matters vapor containing the water vapor is converted into liquid from gas, the liquid is discharged from the first-stage condenser 6 and the second-stage condenser 7, the mixed solution of the liquid water and the organic matters is collected into the solvent collecting tank 11, the condensate discharging pipelines of the first-stage condenser 6 and the second-stage condenser 7 are not provided with valves, the sealing of the condensate discharging pipelines of the first-stage condenser 6 and the second-stage condenser 7 is realized by arranging liquid seals, and the liquid seal height is more than or equal to 500mm.
After desorption of the adsorption tank 4 is completed, the adsorption tank is transferred to a drying and cooling operation, closed drying and cooling are firstly adopted, at the moment, valves 4-1, 4-2, 4-4, 4-5, 4-7, 4-8 and 4-9 of the adsorption tank are all closed, the valves 4-3 and 4-6 are opened, a drying and cooling fan 9 is started, meanwhile, an inlet valve 9-1 of the drying and cooling fan 9 is closed, air enters the adsorption tank 4 after being pressurized by the drying and cooling fan 9, heat and water vapor in the adsorbent of the adsorption tank 4 are purged, organic waste gas in the adsorption tank 4 is taken out, the purged gas enters a drying and cooling air heat exchanger 10, water vapor in the gas phase is condensed into water, the water is discharged into a solvent collecting tank 11 through a purge pipeline of the drying and cooling air heat exchanger 10, the purge pipeline is not provided with a valve, a section of liquid sealing pipe is arranged, the liquid sealing height is at least 500mm, and sealing of the purge pipeline of the drying and cooling air heat exchanger 10 is realized through liquid sealing; the cooled and dehydrated gas returns to the inlet of the drying and cooling fan 9 and is blown into the adsorption tank 4 again to dry and cool the adsorbent again, after a period of circulating drying and cooling, the temperature of the adsorbent in the adsorption tank 4 is reduced, and the organic matters in the drying and cooling air are also re-adsorbed by the adsorbent, so that closed cooling and drying are carried out into open cooling and drying: opening an inlet valve 9-1 of a drying cooling fan 9, opening a valve 4-4, closing a valve 4-6, directly extracting air from the atmosphere by the drying cooling fan 9, drying and cooling the adsorbent in the adsorption tank 4, directly discharging the high-temperature gas containing water vapor which is purged out into an exhaust barrel, and when the temperature of the adsorbent in the adsorption tank 4 is lower than 50 ℃, completing the drying and cooling operation because the organic matters in the gas in the adsorption tank 4 are re-adsorbed by the adsorbent, and the discharged gas meets the environmental protection emission requirement.
When the adsorption tank 4 finishes the desorption and drying cooling operation, the adsorption operation can be switched into, at the moment, the adsorption tank 3 is switched into the primary adsorption, the adsorption tank 4 is switched into the secondary adsorption, and meanwhile, the adsorption tank 2 is switched into the desorption and drying cooling operation, when the adsorption tank 2 finishes the desorption and drying cooling operation, the adsorption tank 4 is switched into the primary adsorption, the adsorption tank 2 is switched into the secondary adsorption, and the adsorption tank 3 is switched into the desorption and drying cooling operation, so as to push, and the three adsorption tanks alternately perform the primary adsorption, the secondary adsorption, the desorption and the drying cooling operation, and repeatedly and continuously run.
The liquid stored in the solvent collection tank 11 is transported outside by the solvent transport pump 12.
Example 3
Referring to fig. 3, the two adsorption and one desorption processes have three adsorption tanks in total, and in normal operation, two adsorption tanks are connected in series for adsorption (the series mode is shown as the figure), and the other adsorption tank is used for desorption, drying and cooling.
The adsorption tank 2 is first-stage adsorbed, the adsorption tank 3 is second-stage adsorbed, and the desorption, drying and cooling of the adsorption tank 4 are described in detail.
The organic waste gas is fed to an inlet of an adsorption tank 2 after being pressurized by an induced draft fan 1, at the moment, an inlet valve 2-2 of the adsorption tank 2 is opened, valves 2-1, 2-3, 2-4, 2-6, 2-7, 2-8 and 2-9 are all closed, an inlet valve 3-1 of the adsorption tank 3 is opened, an outlet valve 3-4 of the adsorption tank 3 is opened, valves 3-2, 3-3, 3-5, 3-6, 3-7, 3-8 and 3-9 are all closed, the organic waste gas sequentially enters the adsorption tank 2 and the adsorption tank 3, passes through an adsorbent layer inside the adsorption tank 2 and the adsorption tank 3, the organic matters are captured and adsorbed by the adsorbent to be removed, the purified gas is discharged from the adsorption tank 3, and the gas enters an exhaust barrel to reach the standard.
The adsorption tank 2 and the adsorption tank 3 are subjected to adsorption operation, the adsorption tank 4 is subjected to desorption operation, water vapor is depressurized to be below 0.1MPa through a valve 5-1 and then enters a vapor buffer tank 5, at the moment, the vapor is superheated vapor, a certain amount of pure water is sprayed into the vapor buffer tank to cool the superheated vapor, the sprayed pure water flow is regulated by regulating the opening degree of the valve 5-3, so that the temperature of the water vapor is controlled, the vapor reaching the required temperature is conveyed to a vapor inlet of the adsorption tank 4, at the moment, a vapor inlet valve 4-7 and a valve 4-9 of the adsorption tank 4 are opened, the valve 4-1, the valve 4-2, the valve 4-3, the valve 4-4, the valve 4-5, the valve 4-6 and the valve 4-8 are all closed, the vapor enters the adsorption tank 4, a part of the vapor is directly condensed into the adsorption tank 4 to be collected to the bottom of the adsorption tank 4, the condensate water at the bottom of the adsorption tank 4 is discharged through a condensate water discharging pipe, the valve is not arranged on the discharging pipe, the sealing of the discharging pipe of the adsorption tank 4 is realized, the condensate water discharging pipe is discharged into a condensate water cooler 11 after the condensate water cooler is cooled by the condensate tank 11, and the condensate water is discharged into the condensate tank 11 after the condensate tank is cooled by the condensate tank at the height of 500 mm; under the continuous sweeping of the water vapor, the organic matters are desorbed from the inside of the adsorbent, the organic matters vapor desorbed from the water vapor enters the first-stage condenser 6 and the second-stage condenser 7 from the adsorption tank 4, the organic matters vapor containing the water vapor is converted into liquid from gas, the liquid is discharged from the first-stage condenser 6 and the second-stage condenser 7, the mixed solution of the liquid water and the organic matters is collected into the solvent collecting tank 11, the condensate discharging pipelines of the first-stage condenser 6 and the second-stage condenser 7 are not provided with valves, the sealing of the condensate discharging pipelines of the first-stage condenser 6 and the second-stage condenser 7 is realized by arranging liquid seals, and the liquid seal height is more than or equal to 500mm.
After desorption of the adsorption tank 4 is completed, the adsorption tank is transferred to a drying and cooling operation, closed drying and cooling are firstly adopted, at the moment, valves 4-1, 4-2, 4-4, 4-5, 4-7, 4-8 and 4-9 of the adsorption tank are all closed, the valves 4-3 and 4-6 are opened, a drying and cooling fan 9 is started, meanwhile, an inlet valve 9-1 of the drying and cooling fan 9 is closed, air enters the adsorption tank 4 after being pressurized by the drying and cooling fan 9, heat and water vapor in the adsorbent of the adsorption tank 4 are purged, organic waste gas in the adsorption tank 4 is taken out, the purged gas enters a drying and cooling air heat exchanger 10, water vapor in the gas phase is condensed into water, the water is discharged into a solvent collecting tank 11 through a purge pipeline of the drying and cooling air heat exchanger 10, the purge pipeline is not provided with a valve, a section of liquid sealing pipe is arranged, the liquid sealing height is at least 500mm, and sealing of the purge pipeline of the drying and cooling air heat exchanger 10 is realized through liquid sealing; the cooled and dehydrated gas returns to the inlet of the drying and cooling fan 9 and is blown into the adsorption tank 4 again to dry and cool the adsorbent again, after a period of circulating drying and cooling, the temperature of the adsorbent in the adsorption tank 4 is reduced, and the organic matters in the drying and cooling air are also re-adsorbed by the adsorbent, so that closed cooling and drying are carried out into open cooling and drying: opening an inlet valve 9-1 of a drying cooling fan 9, opening a valve 4-4, closing a valve 4-6, directly extracting air from the atmosphere by the drying cooling fan 9, drying and cooling the adsorbent in the adsorption tank 4, directly discharging the high-temperature gas containing water vapor which is purged out into an exhaust barrel, and when the temperature of the adsorbent in the adsorption tank 4 is lower than 50 ℃, completing the drying and cooling operation because the organic matters in the gas in the adsorption tank 4 are re-adsorbed by the adsorbent, and the discharged gas meets the environmental protection emission requirement.
When the adsorption tank 4 is subjected to desorption and drying cooling operation, the adsorption operation can be switched into adsorption operation, at the moment, the adsorption tank 3 is switched into primary adsorption, the adsorption tank 4 is switched into secondary adsorption, meanwhile, the adsorption tank 2 is switched into desorption and drying cooling operation, when the adsorption tank 2 is subjected to desorption and drying cooling operation, the adsorption tank 4 is switched into primary adsorption, the adsorption tank 2 is switched into secondary adsorption, the adsorption tank 3 is switched into desorption and drying cooling operation, and the three adsorption tanks alternately perform primary adsorption, secondary adsorption, desorption and drying cooling operation, and continuously run repeatedly.
The liquid stored in the solvent collection tank 11 is transported outside by the solvent transport pump 12.
Example 4
Referring to fig. 4, the two-adsorption-one-desorption process includes three adsorption tanks, and in normal operation, two adsorption tanks are connected in parallel for adsorption, and the other adsorption tank is subjected to desorption, drying and cooling.
The adsorption tank 2 and the adsorption tank 3 are connected in parallel, and the desorption, drying and cooling of the adsorption tank 4 are described in detail.
The organic waste gas is fed to the inlet of the adsorption tank 2 and the inlet of the adsorption tank 3 after being pressurized by the induced draft fan 1, at the moment, the inlet valve 2-1 of the adsorption tank 2 is opened, the outlet valve 2-3 of the adsorption tank 2 is opened, the valves 2-2, 2-4, 2-5, 2-6 and 2-7 are all closed, the inlet valve 3-1 of the adsorption tank 3 is opened, the outlet valve 3-3 of the adsorption tank 3 is opened, the valves 3-2, 3-4, 3-5, 3-6 and 3-7 are all closed, the organic waste gas simultaneously enters the adsorption tank 2 and the adsorption tank 3, after passing through the adsorbent layers inside the adsorption tank 2 and the adsorption tank 3, the organic matters are captured and adsorbed by the adsorbent to be removed, and the purified gas is discharged from the adsorption tank 2 and the adsorption tank 3 and enters an exhaust drum to reach the standard for emission.
The adsorption tank 2 and the adsorption tank 3 are subjected to adsorption operation, the adsorption tank 4 is subjected to desorption operation, water vapor is depressurized to be below 0.1MPa through a valve 5-1 and then enters a vapor buffer tank 5, at the moment, the vapor is superheated vapor, a certain amount of pure water is sprayed into the vapor buffer tank to cool the superheated vapor, the opening of the valve 5-3 is regulated to regulate the flow rate of the sprayed pure water, so that the temperature of the water vapor is controlled, the vapor reaching the required temperature is conveyed to a vapor inlet of the adsorption tank 3, at the moment, a vapor inlet valve 4-5 and a valve 4-7 of the adsorption tank 4 are opened, the valve 4-1, the valve 4-2, the valve 4-3, the valve 4-4 and the valve 4-6 are all closed, the vapor enters the adsorption tank 4, a part of the water vapor is directly condensed into the adsorption tank 4, the bottom of the adsorption tank 4 is collected, the superheated vapor is discharged through a condensed water discharging pipe at the bottom of the adsorption tank 4, the liquid sealing pipe is realized through the liquid sealing, the liquid sealing height of the discharged condensate is not less than or equal to 500mm, and the discharged condensate enters a water cooler 8 of the adsorption tank and is discharged into a cooling and condensed solvent 11 for cooling and collecting tank 11; under the continuous sweeping of the water vapor, the organic matters are desorbed from the inside of the adsorbent, the organic matters vapor desorbed from the water vapor enters the first-stage condenser 6 and the second-stage condenser 7 from the adsorption tank 4, the organic matters vapor containing the water vapor is converted into liquid from gas, the liquid is discharged from the first-stage condenser 6 and the second-stage condenser 7, the mixed solution of the liquid water and the organic matters is collected into the solvent collecting tank 11, the condensate discharging pipelines of the first-stage condenser 6 and the second-stage condenser 7 are not provided with valves, the sealing of the condensate discharging pipelines of the first-stage condenser 6 and the second-stage condenser 7 is realized by arranging liquid seals, and the liquid seal height is more than or equal to 500mm.
After desorption of the adsorption tank 4 is completed, the adsorption tank is transferred to a drying and cooling operation, closed drying and cooling are firstly adopted, at the moment, valves 4-1, 4-3, 4-5, 4-6 and 4-7 of the adsorption tank are closed, the valves 4-2 and 4-4 are opened, a drying and cooling fan 9 is started, meanwhile, an inlet valve 9-1 of the drying and cooling fan 9 is closed, air is pressurized by the drying and cooling fan 9 and enters the adsorption tank 4, heat and water vapor in the adsorbent of the adsorption tank 4 are purged, organic waste gas in the adsorption tank 4 is carried out, the purged gas enters a drying and cooling air heat exchanger 10, water vapor in the gas phase is condensed into water, the water is discharged into a solvent collecting tank 11 through a discharging pipeline of the drying and cooling air heat exchanger 10, the discharging pipeline is not provided with a valve, the liquid sealing height is at least 500mm, and sealing of the discharging pipeline of the drying and cooling air heat exchanger 10 is realized through liquid sealing; the cooled and dehydrated gas returns to the inlet of the drying and cooling fan 9 and is blown into the adsorption tank 4 again to dry and cool the adsorbent again, after a period of circulating drying and cooling, the temperature of the adsorbent in the adsorption tank 4 is reduced, and the organic matters in the drying and cooling air are also re-adsorbed by the adsorbent, so that closed cooling and drying are carried out into open cooling and drying: opening an inlet valve 9-1 of a drying and cooling fan 9, opening a valve 4-3, closing the valve 4-4, directly extracting air from the atmosphere by the drying and cooling fan 9, drying and cooling the adsorbent in the adsorption tank 4, directly discharging the high-temperature gas containing water vapor which is purged into an exhaust barrel, and when the temperature of the adsorbent in the adsorption tank 4 is lower than 50 ℃, completing the drying and cooling operation because the organic matters in the gas in the adsorption tank 4 are re-adsorbed by the adsorbent, and the discharged gas meets the environmental protection emission requirement.
When the adsorption tank 4 is subjected to desorption and drying cooling operation, the adsorption operation can be carried out, at the moment, the adsorption tank 3 and the adsorption tank 4 are connected in parallel for adsorption, the adsorption tank 2 is carried out in desorption and drying cooling operation, when the desorption and drying cooling operation of the adsorption tank 2 is finished, the adsorption tank 3 is carried out in desorption and drying cooling operation, at the moment, the adsorption tank 2 and the adsorption tank 4 are connected in parallel for adsorption, and the like, the three adsorption tanks are alternately connected in parallel for adsorption, desorption and drying cooling operation, and the continuous operation is repeated.
The liquid stored in the solvent collection tank 11 is transported outside by the solvent transport pump 12.
The above embodiments are only for illustrating the inventive concept of the present patent and not for limiting the protection of the patent claims, and all insubstantial modifications of the patent using this concept shall fall within the protection scope of the patent.
Claims (10)
1. An adsorption and water vapor desorption condensation recovery process is applied to an organic waste gas treatment device, and the device comprises an induced draft fan (1), an adsorption tank (2), an adsorption tank (3), an adsorption tank (4), a vapor buffer tank (5), a primary condenser (6), a secondary condenser (7), an adsorption tank condensation water cooler (8), a drying cooling fan (9), a drying cooling air heat exchanger (10), a solvent collection tank (11) and a solvent delivery pump (12); the number of the adsorption tanks (2, 3, 4) is not limited to the number described above, and the number of the adsorption tanks (2, 3, 4) can be n+1 (where n is an integer greater than or equal to 1), and the adsorption tanks (2, 3) can be n in series to adsorb one adsorption tank (4) for desorption, drying and cooling, or the adsorption tanks (2, 3) in parallel to adsorb one adsorption tank (4) for desorption, drying and cooling; the invention will be described by taking 3 adsorption tanks as an example, wherein the process comprises the following steps:
step one: three adsorption tanks (2, 3, 4) are all arranged, wherein two adsorption tanks (2, 3) are connected in series to adsorb desorption, drying and cooling operation of one adsorption tank (4): the organic waste gas is pressurized by an induced draft fan (1) and then sequentially enters adsorption tanks (2 and 3) for adsorption operation, wherein the adsorption tanks (2) are subjected to primary adsorption, the adsorption tanks (3) are subjected to secondary adsorption, when the organic waste gas sequentially passes through adsorbent layers in the adsorption tanks (2 and 3), organic matters in the waste gas are adsorbed by the adsorbent, and when the organic waste gas is discharged from the adsorption tanks (3), the concentration of the organic matters in the waste gas meets the environmental protection discharge requirement and is sent to an exhaust barrel for high-altitude discharge; simultaneously, the desorption operation is carried out on the adsorption tank (4), desorption steam is depressurized to be below 0.1MPa and enters the steam buffer tank (5), at the moment, the steam is superheated steam, the superheated steam enters the adsorption tank (4) which needs to be desorbed after being subjected to spray cooling in the steam buffer tank (5), organic matters are desorbed from the inside of the adsorbent under the purging of the steam, the organic matter steam containing the steam enters the primary condenser (6) and the secondary condenser (7) from the adsorption tank (4), the organic matter steam containing the steam is converted into liquid from gas state, and is collected in the solvent collection tank (11); the adsorption tank (4) after desorption is transferred into a drying and cooling operation, and firstly, the adsorbent in the adsorption tank (4) is subjected to closed cooling and drying: starting a drying cooling fan (9), sweeping out heat and water vapor contained in the adsorbent in the adsorption tank (4), simultaneously taking out organic waste gas in the adsorption tank (4), enabling the swept out gas to enter a drying cooling air heat exchanger (10), removing water vapor condensed in a gas phase after heat exchange cooling, enabling the cooled and dehydrated gas to return to an inlet of the drying cooling fan (9), and blowing the cooled and dehydrated gas into the adsorption tank (4) again to dry and cool the adsorbent again, wherein after a period of cyclic drying cooling, the temperature of the adsorbent in the adsorption tank (4) is reduced, and organic matters in the drying cooling air are also re-adsorbed by the adsorbent, and then transferring closed cooling drying to open cooling drying: opening an inlet valve of a drying cooling fan (9), directly extracting air from the atmosphere by the drying cooling fan (9), drying and cooling the adsorbent in the adsorption tank (4), and directly discharging the high-temperature gas containing water vapor which is purged out into an exhaust barrel, wherein organic matters in the gas in the adsorption tank (4) are re-adsorbed by the adsorbent, so that the discharged gas meets the environmental protection discharge requirement; the adsorption tank (4) with the completed drying and cooling can be put into adsorption operation again, the adsorption saturated adsorption tank (2) is switched into desorption and drying and cooling operation, the adsorption tank (3) is switched into primary adsorption, the adsorption tank (4) is secondary adsorption, after the desorption of the adsorption tank (2) and the drying and cooling operation are completed, the adsorption tank (4) is primary desorption, the adsorption tank (2) is secondary desorption, the adsorption tank (3) is switched into desorption and drying and cooling operation, and the like, a plurality of adsorption tanks (2, 3 and 4) are alternately subjected to series adsorption, desorption and drying and cooling operation, and the continuous operation is repeated;
step two: a total of 3 adsorption tanks (2, 3, 4), wherein two adsorption tanks (2, 3) are connected in parallel to adsorb desorption, drying and cooling operation of one adsorption tank (4): the organic waste gas is pressurized by an induced draft fan (1) and then enters two adsorption tanks (2, 3) at the same time to carry out adsorption operation, wherein the two adsorption tanks (2, 3) are connected in parallel, when the organic waste gas passes through an adsorbent layer in the adsorption tanks (2, 3), organic matters in the waste gas are adsorbed by the adsorbent, and when the organic waste gas is discharged from the adsorption tanks (2, 3), the concentration of the organic matters in the waste gas meets the environmental protection discharge requirement and is sent to an exhaust barrel to be discharged at high altitude; simultaneously, the desorption operation is carried out on the adsorption tank (4), desorption steam is depressurized to be below 0.1MPa and enters the steam buffer tank (5), at the moment, the steam is superheated steam, the superheated steam enters the adsorption tank (4) which needs to be desorbed after being subjected to spray cooling in the steam buffer tank (5), organic matters are desorbed from the inside of the adsorbent under the purging of the steam, the organic matter steam containing the steam enters the primary condenser (6) and the secondary condenser (7) from the adsorption tank (4), the organic matter steam containing the steam is converted into liquid from gas state, and is collected in the solvent collection tank (11); the adsorption tank (4) after desorption is transferred into a drying and cooling operation, and firstly, the adsorbent in the adsorption tank (4) is subjected to closed cooling and drying: starting a drying cooling fan (9), sweeping out heat and water vapor contained in the adsorbent in the adsorption tank (4), simultaneously taking out organic waste gas in the adsorption tank (4), enabling the swept out gas to enter a drying cooling air heat exchanger (10), removing water vapor condensed in a gas phase after heat exchange cooling, enabling the cooled and dehydrated gas to return to an inlet of the drying cooling fan (9), and blowing the cooled and dehydrated gas into the adsorption tank (4) again to dry and cool the adsorbent again, wherein after a period of cyclic drying cooling, the temperature of the adsorbent in the adsorption tank (4) is reduced, and organic matters in the drying cooling air are also re-adsorbed by the adsorbent, and then transferring closed cooling drying to open cooling drying: opening an inlet valve of a drying cooling fan (9), directly extracting air from the atmosphere by the drying cooling fan (9), drying and cooling the adsorbent in the adsorption tank (4), and directly discharging the high-temperature gas containing water vapor which is purged out into an exhaust barrel, wherein organic matters in the gas in the adsorption tank (4) are re-adsorbed by the adsorbent, so that the discharged gas meets the environmental protection discharge requirement; the adsorption tank (4) after drying and cooling can be put into adsorption operation again, the adsorption saturated adsorption tank (2) is transferred into desorption and drying and cooling operation, the adsorption tank (3) and the adsorption tank (4) are connected in parallel for adsorption, and the like, and a plurality of adsorption tanks (2, 3 and 4) are alternately connected in parallel for adsorption, desorption and drying and cooling operation, so that the continuous operation is repeated.
2. The adsorption and vapor desorption condensation recovery process according to claim 1, wherein the design pressure of the adsorption tanks (2, 3, 4) is less than 0.1MPa, and the adsorption tanks are non-pressure vessels; the adsorbents in the adsorption tanks (2, 3, 4) are columnar granular activated carbon, macroporous resin, activated carbon fibers and the like; the adsorption tanks (2, 3, 4) are horizontal double-oval sealing heads, vertical double-oval sealing heads or vertical flat top cone bottom structures.
3. The adsorption and vapor desorption condensation recovery process according to claim 1, wherein the temperature of the desorption vapor is adjusted by a spray attemperation process.
4. The adsorption and vapor desorption condensation recovery process according to claim 1, wherein the vapor is reduced to less than 0.1MPa by one or two stages of pressure reduction, and a pressure reducing valve, a self-standing pressure regulating valve, or a regulating valve can be used.
5. The adsorption and vapor desorption condensation recovery process according to claim 1, wherein the vapor spray water temperature reduction process controls the temperature of vapor by adjusting the amount of water sprayed, and the water inlet valve is a regulating valve or an automatic switching valve.
6. The adsorption and steam desorption condensation recovery process according to claim 1, wherein after the steam enters the adsorption tanks (2, 3, 4), part of the steam is directly condensed into liquid, the liquid is collected at the bottoms of the adsorption tanks (2, 3, 4), flows to the adsorption tank condensate cooler (8) through a drain pipe at the bottoms of the adsorption tanks (2, 3, 4), the cooled liquid is collected in the solvent collection tank (11), and the adsorption tank condensate cooler (8) is a spiral plate type heat exchanger or a graphite heat exchanger.
7. The device according to claim 6, characterized in that the working pressure in the adsorption tank (2, 3, 4) is low, the condensate drain pipes at the bottom of the adsorption tank (2, 3, 4) are not provided with valves, the condensate drain pipes at the bottom of the adsorption tank (2, 3, 4) are all provided with liquid seal pipes, the liquid seal height is at least 500mm, and the sealing of the condensate drain pipes of the adsorption tank (2, 3, 4) is realized through the liquid seal.
8. The adsorption and water vapor desorption condensation recovery process as claimed in claim 1, wherein the working pressure in the primary condenser (6) and the secondary condenser (7) is lower, the condensate outlet pipelines of the primary condenser (6) and the secondary condenser (7) are not provided with valves, a section of liquid seal pipe is arranged, the liquid seal height is at least 500mm, and the sealing of the condensate outlet pipelines of the primary condenser (6) and the secondary condenser (7) is realized through liquid seal; the desorption waste gas is subjected to a two-stage condensation process through a first-stage condenser (6) and a second-stage condenser (7), and when the boiling point of the desorbed organic matters is higher, the requirement can be met by adopting the single-stage condensation of the first-stage condenser (6); the primary condenser (6) and the secondary condenser (7) are vertical or horizontal shell-and-tube heat exchangers, and can also be vertical or horizontal graphite heat exchangers.
9. The adsorption and water vapor desorption condensation recovery process according to claim 1, wherein the dry cooling air heat exchanger (10) is a tube fin type heat exchanger or a graphite heat exchanger; the inlet valve of the drying cooling fan (9) is an automatic valve or a check valve; after the water vapor is condensed into liquid water in the drying and cooling air heat exchanger (10), the liquid water is discharged through a drying and cooling air heat exchanger (10) exhaust pipeline, and as the working pressure of the drying and cooling air heat exchanger (10) is lower, a valve is not arranged on the exhaust pipeline, a section of liquid seal pipe is arranged, the liquid seal height is at least 500mm, and the sealing of the drying and cooling air heat exchanger (10) exhaust pipeline is realized through liquid seal.
10. The adsorption and water vapor desorption condensation recovery process according to claim 1, wherein condensed water at the bottom of the adsorption tank (2, 3, 4), condensed water discharged from the primary condenser (6) and the secondary condenser (7) and condensed water discharged from the drying cooling air heat exchanger (10) are collected and discharged into the solvent collection tank (11), and are transported outwards through the solvent delivery pump (12); the top emptying pipeline of the solvent collection tank (11) is connected to the organic waste gas inlet main pipe of the adsorption and water vapor desorption condensation recovery device, so that direct emptying is avoided.
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