CN117599565A - Condensing adsorption recovery system for methylene dichloride gas - Google Patents
Condensing adsorption recovery system for methylene dichloride gas Download PDFInfo
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- CN117599565A CN117599565A CN202311732575.8A CN202311732575A CN117599565A CN 117599565 A CN117599565 A CN 117599565A CN 202311732575 A CN202311732575 A CN 202311732575A CN 117599565 A CN117599565 A CN 117599565A
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- 238000001179 sorption measurement Methods 0.000 title claims abstract description 332
- YMWUJEATGCHHMB-UHFFFAOYSA-N Dichloromethane Chemical compound ClCCl YMWUJEATGCHHMB-UHFFFAOYSA-N 0.000 title claims abstract description 300
- 238000011084 recovery Methods 0.000 title claims abstract description 67
- 238000005057 refrigeration Methods 0.000 claims abstract description 94
- 239000011347 resin Substances 0.000 claims abstract description 86
- 229920005989 resin Polymers 0.000 claims abstract description 86
- 238000009833 condensation Methods 0.000 claims abstract description 54
- 230000005494 condensation Effects 0.000 claims abstract description 54
- 238000001816 cooling Methods 0.000 claims abstract description 47
- 238000010257 thawing Methods 0.000 claims abstract description 37
- 230000005540 biological transmission Effects 0.000 claims abstract description 18
- 239000007789 gas Substances 0.000 claims description 204
- 239000007788 liquid Substances 0.000 claims description 177
- 238000010926 purge Methods 0.000 claims description 59
- 238000003795 desorption Methods 0.000 claims description 45
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 40
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 22
- 239000003463 adsorbent Substances 0.000 claims description 21
- 229910052757 nitrogen Inorganic materials 0.000 claims description 20
- 239000003507 refrigerant Substances 0.000 claims description 19
- 229910000831 Steel Inorganic materials 0.000 claims description 17
- 239000010959 steel Substances 0.000 claims description 17
- 239000000110 cooling liquid Substances 0.000 claims description 16
- 238000010438 heat treatment Methods 0.000 claims description 14
- 238000000926 separation method Methods 0.000 claims description 13
- 238000004200 deflagration Methods 0.000 claims description 10
- 239000010865 sewage Substances 0.000 claims description 9
- 229920000642 polymer Polymers 0.000 claims description 7
- 229910052573 porcelain Inorganic materials 0.000 claims description 6
- 238000001914 filtration Methods 0.000 claims description 5
- BDERNNFJNOPAEC-UHFFFAOYSA-N propan-1-ol Chemical compound CCCO BDERNNFJNOPAEC-UHFFFAOYSA-N 0.000 claims description 3
- 230000007797 corrosion Effects 0.000 abstract description 8
- 238000005260 corrosion Methods 0.000 abstract description 8
- 238000000034 method Methods 0.000 description 16
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 13
- 238000011282 treatment Methods 0.000 description 12
- 239000002912 waste gas Substances 0.000 description 12
- 239000002826 coolant Substances 0.000 description 11
- 230000008569 process Effects 0.000 description 10
- 230000008929 regeneration Effects 0.000 description 10
- 238000011069 regeneration method Methods 0.000 description 10
- 208000028659 discharge Diseases 0.000 description 7
- 239000000243 solution Substances 0.000 description 6
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- 239000000203 mixture Substances 0.000 description 5
- 239000000498 cooling water Substances 0.000 description 4
- 230000008439 repair process Effects 0.000 description 4
- 238000009835 boiling Methods 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 238000006073 displacement reaction Methods 0.000 description 3
- 238000002474 experimental method Methods 0.000 description 3
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
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- 238000003466 welding Methods 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 125000003118 aryl group Chemical group 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
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- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
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- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
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- 239000012855 volatile organic compound Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- 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
- B01D53/002—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 condensation
-
- 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
- B01D53/0462—Temperature swing adsorption
-
- 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
- B01D2257/20—Halogens or halogen compounds
- B01D2257/206—Organic halogen compounds
- B01D2257/2064—Chlorine
-
- 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
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Separation Of Gases By Adsorption (AREA)
Abstract
The invention discloses a condensation adsorption recovery system for methylene dichloride gas, which comprises a gas transmission unit, a gas-gas heat recovery unit, a main condensation unit, a carrier unit, a refrigeration unit, a resin adsorption unit, an analysis cooling unit connected with the resin adsorption unit and an exhaust unit connected with the resin adsorption unit; the system is also provided with a carrier refrigeration cycle system and a carrier defrosting cycle system; the refrigerating unit provides cold for the refrigerating medium in the carrier refrigerating cycle system and provides heat for the heat carrier in the carrier defrosting cycle system; the carrier refrigeration cycle system provides cold energy for the main condensing unit, and the carrier defrosting cycle system provides heat for the main condensing unit. The Freon refrigeration cycle of the refrigeration unit realizes indirect condensation of the main condenser through the refrigerating medium, and realizes indirect defrosting of the main condenser through the heat carrier, thereby effectively reducing the risk of corrosion pollution in the Freon refrigeration cycle and being safer and more reliable.
Description
Technical Field
The invention belongs to the technical field of waste gas treatment, and particularly relates to a condensation adsorption recovery system for gas.
Background
With the stricter emission standard of VOCs, the emission standard of pollutants in petrochemical industry GB31571-2015 requires that the removal rate of non-methane total hydrocarbon of an organic waste gas discharge port is more than or equal to 97 percent, and the emission limit of organic characteristic pollutant methylene dichloride in waste gas is 100mg/m 3 。
Dichloromethane (CH) 2 Cl 2 ) Boiling point 39.8 ℃ and is colorlessTransparent volatile liquid has an aromatic smell with a pungent smell, is toxic during inhalation, has a low boiling point and is easy to volatilize, steam and air of the transparent volatile liquid can form an explosive mixture, and the volatile liquid is easy to volatilize during industrial production to cause environmental pollution. The dried methylene chloride is non-corrosive but is corrosive to water (due to the free chlorine Cl - So it is corrosive), its strength is dependent on Cl - The content varies. Cl - Is a main cause of pitting corrosion and crevice corrosion of stainless steel, and can cause perforation accidents when severe, the characteristic of dichloromethane is particularly unfavorable for a refrigeration unit in a gas condensation adsorption recovery process, meanwhile, the Freon refrigerating system of the refrigerating unit is mostly welded because of being incapable of leakage, and equipment maintenance and replacement are very difficult.
Therefore, in the recovery of the dichloromethane gas/waste gas, how to obtain a recovery process which can safely liquefy the dichloromethane, can also realize environmental protection and discharge, and can greatly reduce or even avoid corrosion, pollution or leakage to the freon refrigerating system of the refrigerating unit is worthy of research and needs to be solved.
Disclosure of Invention
The invention aims to: in order to overcome the defects in the prior art, the invention provides a condensation adsorption recovery system for methylene dichloride gas.
The technical scheme is as follows: the invention provides a condensation adsorption recovery system for methylene dichloride gas, which comprises a gas transmission unit, a gas-gas heat recovery unit connected with a gas transmission unit gas circuit, a main condensation unit connected with the gas-gas heat recovery unit gas circuit, a carrier unit connected with the main condensation unit, a refrigeration unit connected with the carrier unit, a resin adsorption unit connected with the gas-gas heat recovery unit, an analysis cooling unit connected with the resin adsorption unit and an exhaust unit connected with the resin adsorption unit;
the resin adsorption unit is provided with an adsorption bypass valve; the air inlet end of the adsorption bypass valve is connected with the main condensing unit, and the air outlet end of the adsorption bypass valve is connected with the exhaust unit;
the system is also provided with a carrier refrigeration cycle system and a carrier defrosting cycle system; the refrigerating unit provides cold for the refrigerating medium in the carrier refrigerating cycle system and provides heat for the heat carrier in the carrier defrosting cycle system; the carrier refrigeration cycle system provides cold energy for the main condensing unit, and the carrier defrosting cycle system provides heat for the main condensing unit.
Further preferably, the carrier unit comprises an intermediate heat exchanger, a carrier cooling pump, a carrier cooling liquid inlet valve A, a carrier cooling liquid inlet valve B, a carrier cooling liquid outlet valve A, a carrier cooling liquid outlet valve B, a carrier cooling expansion tank, a carrier heat pump, a carrier heating liquid inlet valve A, a carrier heating liquid inlet valve B, a carrier heating liquid outlet valve A, a carrier heating liquid outlet valve B and a carrier heating expansion tank;
the carrier refrigeration cycle system comprises: the cold-carrying liquid outlet valve A and the cold-carrying liquid outlet valve B are arranged in parallel, the intermediate heat exchanger, the cold-carrying pump, and the cold-carrying liquid inlet valve A and the cold-carrying liquid inlet valve B are arranged in parallel;
the vehicle defrosting circulation system comprises the following components connected in sequence: the heat-carrying liquid outlet valve A and the heat-carrying liquid outlet valve B are arranged in parallel, the subcooler, the heat-carrying pump, and the heat-carrying liquid inlet valve A and the heat-carrying liquid inlet valve B are arranged in parallel.
Still further preferably, the cold liquid at the outlet of the cold carrying pump can be sent to the carrier inlet of the main condenser A through the cold carrying liquid inlet valve A, the carrier outlet of the main condenser A is connected with the cold carrying liquid outlet valve A, the other end of the cold carrying liquid outlet valve A is connected with the cold carrying inlet of the intermediate heat exchanger, and the cold carrying outlet of the intermediate heat exchanger is connected with the inlet of the cold carrying pump;
the outlet cold liquid of the cold carrying pump can be sent to the carrier inlet of the main condenser B through the cold carrying liquid inlet valve B, the carrier outlet of the main condenser B is connected with the cold carrying liquid outlet valve B, the other end of the cold carrying liquid outlet valve B is connected with the cold carrying inlet of the intermediate heat exchanger, and the cold carrying outlet of the intermediate heat exchanger is connected with the inlet of the cold carrying pump;
The outlet hot liquid of the heat carrier pump can be sent into the carrier inlet of the main condenser A through the heat carrier liquid inlet valve A, the carrier outlet of the main condenser A is connected with the heat carrier liquid outlet valve A, the other end of the heat carrier liquid outlet valve A is connected with the heat carrier inlet of the subcooler, and the heat carrier outlet of the subcooler is connected with the inlet of the heat carrier pump;
the outlet hot liquid of the heat carrier pump can be sent into the carrier inlet of the main condenser B through the heat carrier liquid inlet valve B, the carrier outlet of the main condenser B is connected with the heat carrier liquid outlet valve B, the other end of the heat carrier liquid outlet valve B is connected with the heat carrier inlet of the subcooler, and the heat carrier outlet of the subcooler is connected with the inlet of the heat carrier pump.
Preferably, DLJ type high polymer adsorption resin is used as the adsorbent in the resin adsorption unit.
Preferably, the devices in the carrier unit are flanged.
Preferably, both the heat carrier and the coolant are propanol.
Preferably, a grating plate is arranged at the bottom of each adsorption tank in the resin adsorption unit, and a first filtering wire mesh layer, a second wire mesh layer and a third wire mesh layer are sequentially arranged on the grating plate from bottom to top; wherein, a first layer of porcelain balls are filled between the first filtering silk screen layer and the second steel wire mesh layer; resin adsorbents are filled between the second steel wire mesh layer and the third steel wire mesh layer; and a second layer of porcelain balls are laid on the third steel wire mesh layer.
Preferably, the first filter screen layer is a 50 mesh 254SMO steel filter screen.
Preferably, the gas transmission unit comprises a gas transmission induced draft fan and a deflagration-resistant gas inlet flame arrester connected with a gas path of the gas transmission induced draft fan; an oil gas pressure transmitter is also arranged on the gas pipeline of the gas inlet flame arrester, the gas inlet end of which is connected with the methylene dichloride gas inlet; and/or
Spherical adsorption resin with the diameter of 0.3-1.2 mm is adopted as an adsorbent in an adsorption tank of the resin adsorption unit.
Preferably, the air-air heat recovery unit comprises an air-air heat recovery device, the air inlet end of the hot side of the air-air heat recovery device is connected with the air-transmission induced draft fan, the air outlet end of the hot side of the air-air heat recovery device is connected with the air inlet end of the main condensing unit, the air outlet end of the main condensing unit is connected with the air inlet end of the cold side of the air-air heat recovery device, and the liquid outlet of the air-air heat recovery device is connected with the liquid inlet of the coalescer.
Preferably, the main condensing unit comprises an air passage switching valve A, an air passage switching valve B, a main condenser A, a main condenser B, a one-way valve A, a one-way valve B and a coalescer;
the gas channel inlets of the gas channel switching valve A and the gas channel switching valve B are communicated with the hot side air outlet end of the gas-gas heat regenerator; the liquid outlets of the main condenser A and the main condenser B are communicated with the coalescer; the coalescer separates out sewage and dichloromethane and then outputs the sewage and dichloromethane respectively;
The air channel outlet of the air channel switching valve A is communicated with the air inlet end of the main condenser A, the air outlet end of the main condenser A is communicated with the air inlet end of the one-way valve A, and the air outlet end of the one-way valve A is connected with the cold side air inlet end of the air-air heat regenerator;
the air passage outlet of the air passage switching valve B is communicated with the air inlet end of the main condenser B; the air outlet end of the main condenser B is communicated with the air inlet end of the one-way valve B, and the air outlet end of the one-way valve B is connected with the cold side air inlet end of the air-air heat regenerator.
Preferably, one end of the cold-carrying liquid inlet valve A and one end of the heat-carrying liquid inlet valve A are connected with the carrier inlet of the main condenser A, and one end of the cold-carrying liquid outlet valve A and one end of the heat-carrying liquid outlet valve A are connected with the carrier outlet of the main condenser A;
one end of the cold-carrying liquid inlet valve B and one end of the heat-carrying liquid inlet valve B are connected with the carrier inlet of the main condenser B, and one end of the cold-carrying liquid outlet valve B and one end of the heat-carrying liquid outlet valve B are connected with the carrier outlet of the main condenser B.
Further preferably, the resin adsorption unit includes an adsorption tank a, an adsorption tank B, an adsorption tank C, an adsorption inlet valve a, an adsorption inlet valve B, an adsorption inlet valve C, an adsorption outlet valve a, an adsorption outlet valve B, an adsorption outlet valve C, an analysis inlet valve a, an analysis inlet valve B, an analysis inlet valve C, a purge inlet valve a, a purge inlet valve B, a purge inlet valve C, an analysis outlet valve a, an analysis outlet valve B, an analysis outlet valve C, and an adsorption bypass valve;
The cold side air outlet end of the air-air heat regenerator is communicated with one end of the adsorption bypass valve, one end of the adsorption inlet valve A, one end of the adsorption inlet valve B and one end of the adsorption inlet valve C; the other end of the adsorption bypass valve is communicated with the exhaust unit; the other end of the adsorption inlet valve A is communicated with the lower end of the adsorption tank A, the other end of the adsorption inlet valve B is communicated with the lower end of the adsorption tank B, and the other end of the adsorption inlet valve C is communicated with the lower end of the adsorption tank C;
the upper end of the adsorption tank A is communicated with one end of the adsorption outlet valve A, the upper end of the adsorption tank B is communicated with one end of the adsorption outlet valve B, and the upper end of the adsorption tank C is communicated with one end of the adsorption outlet valve C;
the other end of the adsorption-out valve A, the other end of the adsorption-out valve B and the other end of the adsorption-out valve C are communicated with the exhaust unit;
one end of the analysis inlet valve A is communicated with the upper end of the adsorption tank A, one end of the analysis inlet valve B is communicated with the upper end of the adsorption tank B, and one end of the analysis inlet valve C is communicated with the upper end of the adsorption tank C; the other end of the analysis inlet valve A, the other end of the analysis inlet valve B and the other end of the analysis inlet valve C are communicated with a desorption/analysis steam inlet;
one end of the purging inlet valve A is communicated with the upper end of the adsorption tank A, one end of the purging inlet valve B is communicated with the upper end of the adsorption tank B, and one end of the purging inlet valve C is communicated with the upper end of the adsorption tank C; the other end of the purge inlet valve A, the other end of the purge inlet valve B and the other end of the purge inlet valve C are communicated with a nitrogen inlet for desorption/purging;
One end of the analysis outlet valve A is communicated with the lower end of the adsorption tank A, one end of the analysis outlet valve B is communicated with the lower end of the adsorption tank B, and one end of the analysis outlet valve C is communicated with the lower end of the adsorption tank C;
the other end of the analysis outlet valve A, the other end of the analysis outlet valve B and the other end of the analysis outlet valve C are communicated with the input end of the multistage cooler of the analysis cooling unit.
Preferably, the exhaust unit comprises an emptying cylinder, a deflagration-resistant outlet flame arrester and a concentration detector; the concentration detector is arranged in the middle of the tube body of the emptying tube;
and an air inlet of the exhaust funnel is communicated with the other end of the adsorption bypass valve, the other end of the adsorption outlet valve A, the other end of the adsorption outlet valve B and the other end of the adsorption outlet valve C through a deflagration-resistant outlet flame arrester.
Preferably, the analytical cooling unit comprises a multistage cooler and a coalescing separator tank;
the cold source of the multistage cooler is circulating cooling water or circulating chilled water; the air outlet end of the multistage cooler is connected with the air inlet end of the explosion-proof air inlet flame arrester; the liquid outlet end of the multistage cooler is communicated with the liquid inlet end of the coalescence-separation tank;
and the coalescence-separation tank is used for separating and treating dichloromethane and water and then outputting the dichloromethane and the water respectively.
Preferably, the refrigeration unit comprises a refrigeration compressor, a water-cooled condenser, a subcooler and a refrigeration throttling device which are connected in sequence;
the other end of the refrigeration throttling device is communicated with a refrigerant inlet of the intermediate heat exchanger, and a refrigerant outlet of the intermediate heat exchanger is communicated with an input end of the refrigeration compressor;
the cold source of the water-cooled condenser is circulating cooling water;
the heat-carrying outlet of the subcooler is communicated with the inlet of the heat-carrying pump, and the heat-carrying inlet of the subcooler is communicated with the other end of the heat-carrying liquid outlet valve A and the other end of the heat-carrying liquid outlet valve B.
The beneficial effects are that: compared with the prior art, the condensing adsorption recovery system for the methylene dichloride gas has the following advantages:
(1) Based on the structure and the structure provided by the invention, the Freon refrigeration cycle of the refrigeration unit realizes indirect condensation of the main condenser through the refrigerating medium, and the Freon refrigeration cycle of the refrigeration unit realizes indirect defrosting of the main condenser through the heat carrier, thereby ensuring the stability of the temperature of the multi-stage cold field of the main condenser. Experiments prove that the concentration of the methylene dichloride at the air outlet end of the main condenser can be stabilized at 10g/m 3 About, the resin is safely fed into the resin adsorption unit after the subsequent (returned to the gas-gas regenerator) recovery temperature rise, and the concentration of dichloromethane after high-efficiency resin adsorption can reach 60mg/m 3 In the following, the environment-friendly standard emission is realized.
(2) Based on the structure and the structure provided by the invention, the condensation is indirect condensation, and during condensation, the Freon refrigerant in the refrigeration unit does not exchange heat with the dichloromethane tail gas by using one heat exchanger (the Freon refrigeration cycle provides cold for the intermediate heat exchanger; the Freon refrigerant in the Freon refrigeration cycle exchanges heat with the refrigerating medium in the carrier refrigeration cycle in the intermediate heat exchanger and exchanges heat with dichloromethane gas/tail gas in the main condenser of the main condensation unit), so that not only is the corrosion/pollution caused by aqueous dichloromethane solution to the heat exchanger in the Freon refrigeration cycle of the refrigeration unit (the intermediate heat exchanger in the Freon refrigeration cycle) effectively avoided, but also the risk of direct pollution caused by the aqueous dichloromethane solution to the Freon refrigerant is greatly reduced, the risk of leakage of the Freon refrigeration system is effectively avoided/relieved, the possibility of site repair fire operation of the Freon refrigeration cycle of the refrigeration unit is effectively avoided/reduced, and the site repair fire operation of the Freon refrigeration cycle of the refrigeration unit is safer and more reliable.
(3) Based on the structure and the structure provided by the invention, when defrosting is performed indirectly, the freon refrigerant in the refrigerating unit does not exchange heat with the dichloromethane tail gas by using one heat exchanger (the freon refrigerating cycle provides heat for the subcooler; the freon refrigerant in the freon refrigerating cycle exchanges heat with the heat carrier in the carrier defrosting cycle in the subcooler and the carrier defrosting cycle exchanges heat with dichloromethane gas/tail gas in the main condenser of the main condensing unit), so that corrosion/pollution caused by aqueous dichloromethane solution to the heat exchanger in the freon refrigerating cycle of the refrigerating unit (the subcooler in the freon refrigerating cycle) is effectively avoided, the risk of direct pollution caused by the aqueous dichloromethane solution to the freon refrigerant is greatly reduced, the risk of leakage of the freon refrigerating system is effectively avoided/relieved, and the possibility of on-site repair welding operation of the freon refrigerating cycle of the refrigerating unit is also effectively avoided/reduced.
(4) The invention directly condenses the methylene dichloride gas/tail gas by the refrigerating medium in the carrier refrigeration cycle, the temperature difference between the refrigerating medium entering and exiting the same main condenser is about 5 ℃, the refrigerating medium is in closed circulation without phase change in the carrier refrigeration cycle, the condensation temperature fluctuation of the methylene dichloride tail gas is small, and the system operation temperature is stable.
(5) Based on the structure and the structure provided by the invention, the cold energy of dichloromethane gas/tail gas can be recycled through the gas-gas heat regenerator (also called as a gas-cooling recoverer): the methylene dichloride gas/tail gas at the normal temperature of about 30 ℃ enters a gas regenerator device, is primarily precooled and cooled to 6+/-3 ℃ in the gas regenerator 201, then enters a main condenser for multistage cooling to-65+/-5 ℃, then the low-concentration methylene dichloride gas/tail gas is returned to the gas regenerator 201 again to the temperature of 20-25 ℃, and the low-concentration methylene dichloride gas/tail gas at the normal temperature enters a resin adsorption unit from a condensation recovery unit; the cold energy of the air channel is efficiently recycled in the process, and meanwhile, related equipment for providing a cold source for the configuration of the air regenerator is not needed, so that the configuration of the load of the main cooler is reduced, the power consumption of the whole device is greatly reduced, and the energy-saving and environment-friendly effects are achieved.
(6) Furthermore, the main condenser is connected in parallel in a double-way manner, and when the water vapor in the dichloromethane gas/tail gas frosts at low temperature to block the waste gas channel, the two paths can be alternately switched for use (the two paths are controlled to be alternately switched through the gas path switching valve A and the gas path switching valve B), so that the continuous operation of the whole system operation is stably ensured.
(7) The saturated methylene dichloride air inlet experiment at 5 ℃ shows that the methylene dichloride gas/tail gas can be condensed into more than 97 percent of methylene dichloride in a main condenser in a multistage temperature reduction way, the condensate is a mixture of the methylene dichloride and a small amount of water, the mixture flows into a coalescer to be cached by gravity, and more than 95 percent of water is removed through the processes of caching, standing, coalescing, separating and the like (the solubility of the methylene dichloride in the water is 1.38 g-2 g/100mL. H) 2 O), the quality of the condensate is greatly improved, so that the condensate can be better recycled.
(8) Further, based on the structure and the structure of the condensation adsorption recovery system for methylene dichloride gas, the traditional pressure swing adsorption (after normal temperature adsorption, then high temperature desorption and then purging and cooling) can be replaced by temperature swing adsorption (after normal temperature adsorption, vacuum pump is used for pumping and desorption), on one hand, specific resin adsorbent is selected for normal temperature adsorption, on the other hand, high temperature steam is used for desorption/analysis, and on the other hand, nitrogen is used for purging and cooling, when the resin adsorbent is purged by nitrogen, fine adsorbent can enter a sewage tank together with water, cannot be discharged into the air to pollute the environment, the problems that carbon ash is generated by activated carbon under the action of pressure when the traditional activated carbon adsorbent is desorbed and the exhaust cylinder blows black smoke outwards when the activated carbon adsorbent is adsorbed, and the vacuum pump and the adsorption valve are easy to be blocked by the carbon ash generated by the activated carbon adsorbent are effectively improved, so that the system is green and environment-friendly, the safety is higher, and meanwhile, the maintenance cost is effectively reduced.
(9) In the condensing adsorption recovery system for the methylene dichloride gas, a specific resin adsorbent is selected and vapor is used for desorption, so that vacuumizing is not needed, equipment such as a vacuum pump and a cooling system required by a traditional desorption mode is not needed, the problem that the wall thickness of an adsorption tank is required to be increased in order to meet the safety requirement in the traditional active carbon desorption process is solved, the wall thickness of the adsorption tank in the condensing adsorption recovery system for the methylene dichloride gas is not required to be increased, equipment and a structure are more compact, ingenious and reasonable, and meanwhile, the equipment cost is greatly reduced; meanwhile, the resin is adopted for adsorption, so that the method has hydrophobicity, the problem that the adsorption performance of the conventional activated carbon is obviously reduced after multiple blowing-off regeneration is solved, and the tail gas does not reach the standard, and the method has the advantages of no influence on the performance of the resin adsorbent with hydrophobicity by the dichloromethane tail gas humidity and the moisture, stable adsorption performance, easiness in regeneration and no need of replacement, and effectively reduces the generation of a large amount of dangerous wastes.
Drawings
Fig. 1 is a schematic structural diagram of one of the condensation adsorption recovery systems for methylene chloride gas provided in this embodiment.
In the figure, a 100-gas transmission unit, a 200-gas heat recovery unit, a 300-main condensation unit, a 400-resin adsorption unit 500-exhaust unit, a 600-refrigeration unit, a 700-carrier unit and an 800-analytic cooling unit; 101-gas transmission induced draft fan, 102-gas inlet flame arrestor, 103-oil gas pressure transmitter, 201-gas heat regenerator A, 301-gas circuit switching valve A, 302-gas circuit switching valve B, 303-main condenser A, 304-main condenser B, 305-check valve A, 306-check valve B, 307-coalescer; 401-adsorption tank A, 402-adsorption tank B, 403-adsorption tank C, 404-adsorption inlet valve A, 405-adsorption inlet valve B, 406-adsorption inlet valve C, 407-adsorption outlet valve A, 408-adsorption outlet valve B, 409-adsorption outlet valve C, 410-desorption inlet valve A, 411-desorption inlet valve B, 412-desorption inlet valve C, 413-purge inlet valve A, 414-purge inlet valve B, 415-purge inlet valve C, 416-desorption valve A, 417-desorption valve B, 418-desorption valve C, 419-adsorption bypass valve; 501-an emptying cylinder, 502-a deflagration-resistant outlet flame arrester and 503-a concentration detector; 601-a refrigeration compressor, 602-a water-cooled condenser, 603-a subcooler and 604-a refrigeration throttling device; 701-an intermediate heat exchanger, 702-a load cooling pump, 703-a load cooling liquid inlet valve A, 704-a load cooling liquid inlet valve B, 705-a load cooling liquid outlet valve A, 706-a load cooling liquid outlet valve B, 707-a load cooling expansion tank, 708-a load heat pump, 709-a load heat liquid inlet valve A, 710-a load heat liquid inlet valve B, 711-a load heat liquid outlet valve A, 712-a load heat liquid outlet valve B, 713-a load heat expansion tank; 801-multistage coolers, 802-coalescing separator tanks.
Detailed Description
The present invention will be described in further detail with reference to the following examples and drawings, which are not to be construed as limiting the invention.
The condensation adsorption recovery system for dichloromethane gas provided in this embodiment, as shown in fig. 1, includes a gas transmission unit 100, a gas regeneration unit 200 connected to a gas path of the gas transmission unit 100, a main condensation unit 300 connected to a gas path of the gas regeneration unit 200, a carrier unit 700 connected to a carrier pipeline of the main condensation unit 300, a refrigeration unit 600 connected to the carrier unit 700 (that is, the refrigeration unit 600 exchanging heat with the carrier unit 700), a resin adsorption unit 400 connected to the gas regeneration unit 200, a desorption cooling unit 800 connected to the resin adsorption unit 400, and an exhaust unit 500 connected to the resin adsorption unit 400;
wherein the resin adsorption unit 400 is provided with an adsorption bypass valve 419; the air inlet end of the adsorption bypass valve 419 is connected with the main condensing unit 300, and the air outlet end is connected with the exhaust unit 500;
the condensing adsorption recovery system for dichloromethane gas provided by the embodiment is also provided with a carrier refrigeration cycle system and a carrier defrosting cycle system; the refrigeration unit 600 provides cooling capacity for the coolant in the coolant refrigeration cycle and heat for the coolant in the coolant defrost cycle; the carrier refrigeration cycle provides cold to the main condensing unit 300, and the carrier defrost cycle provides heat to the main condensing unit 300, specifically:
The carrier unit 700 includes an intermediate heat exchanger 701, a carrier cooling pump 702, a carrier cooling liquid inlet valve a703, a carrier cooling liquid inlet valve B704, a carrier cooling liquid outlet valve a705, a carrier cooling liquid outlet valve B706, a carrier cooling expansion tank 707, a carrier heat pump 708, a carrier heat liquid inlet valve a709, a carrier heat liquid inlet valve B710, a carrier heat liquid outlet valve a711, a carrier heat liquid outlet valve B712, and a carrier heat expansion tank 713;
the carrier refrigeration cycle system comprises: a cold-carrying liquid outlet valve A705 and a cold-carrying liquid outlet valve B706 which are arranged in parallel, an intermediate heat exchanger 701, a cold-carrying pump 702, a cold-carrying liquid inlet valve A703 and a cold-carrying liquid inlet valve B704 which are arranged in parallel;
the outlet cold liquid of the cold-carrying pump 702 can be sent to the carrier inlet of the main condenser A303 through the cold-carrying liquid inlet valve A703, the carrier outlet of the main condenser A303 is connected with the cold-carrying liquid outlet valve A705, the other end of the cold-carrying liquid outlet valve A705 is connected with the cold-carrying inlet of the intermediate heat exchanger 701, and the cold-carrying outlet of the intermediate heat exchanger 701 is connected with the inlet of the cold-carrying pump 702;
the outlet cold liquid of the cold-carrying pump 702 can be sent to the carrier inlet of the main condenser B304 through the cold-carrying liquid inlet valve B704, the carrier outlet of the main condenser B304 is connected with the cold-carrying liquid outlet valve B706, the other end of the cold-carrying liquid outlet valve B706 is connected with the cold-carrying inlet of the intermediate heat exchanger 701, and the cold-carrying outlet of the intermediate heat exchanger 701 is connected with the inlet of the cold-carrying pump 702;
The vehicle defrosting circulation system comprises the following components connected in sequence: heat carrier liquid outlet valve a711 and heat carrier liquid outlet valve B712, subcooler 603, heat carrier pump 708, heat carrier liquid inlet valve a709 and heat carrier liquid inlet valve B710 arranged in parallel;
the hot liquid at the outlet of the heat-carrying pump 708 can be sent to the carrier inlet of the main condenser A303 through the heat-carrying liquid inlet valve A709, the carrier outlet of the main condenser A303 is connected with the heat-carrying liquid outlet valve A711, the other end of the heat-carrying liquid outlet valve A711 is connected with the heat-carrying inlet of the subcooler 603, and the heat-carrying outlet of the subcooler 603 is connected with the inlet of the heat-carrying pump 708;
the hot liquid at the outlet of the heat-carrying pump 708 can be sent to the carrier inlet of the main condenser B304 through the heat-carrying liquid inlet valve B710, the carrier outlet of the main condenser B304 is connected with the heat-carrying liquid outlet valve B712, the other end of the heat-carrying liquid outlet valve B712 is connected with the heat-carrying inlet of the subcooler 603, and the heat-carrying outlet of the subcooler 603 is connected with the inlet of the heat-carrying pump 708.
In some preferred embodiments, as shown in fig. 1, a cold-carrying expansion tank 707 is disposed on a pipeline connecting the intermediate heat exchanger 701 and the cold-carrying pump 702. In some preferred embodiments, a heat-carrying expansion tank 713 is disposed on the pipeline connecting the subcooler 603 and the heat-carrying pump 708.
In the condensation adsorption recovery system for dichloromethane gas provided in this embodiment, the devices in the carrier unit 700 are connected by flanges; the heat carrier and the secondary refrigerant are both propanol.
In some preferred embodiments, the bottom of the adsorption bed layer of each adsorption tank in the resin adsorption unit 400 is provided with a grating plate to ensure strength, and a first filtering wire mesh layer, a second wire mesh layer and a third wire mesh layer are sequentially arranged above the grating plate from bottom to top; the first layer of porcelain balls are filled between the first filtering silk screen layer and the second steel wire mesh layer to play roles in compressing and equalizing flow; a resin adsorbent (namely an adsorption resin bed layer is formed and used for adsorbing a solvent dichloromethane) is filled between the second steel wire mesh layer and the third steel wire mesh layer; the second layer of porcelain balls are paved on the third steel wire mesh layer to prevent splashing when being adsorbed, so that the current stabilizing effect is achieved. In certain preferred embodiments, the first filter screen layer is a 50 mesh 254SMO steel filter screen for leak protection.
In this embodiment, DLJ-type high polymer adsorbent resin is used as the adsorbent in the adsorption tank of the above-described resin adsorption unit 400. In some preferred embodiments, spherical adsorption resin with a diameter of 0.3-1.2 mm is used as the adsorbent in the adsorption tanks of the resin adsorption unit 400.
In this embodiment, the gas delivery unit 100 includes a gas delivery induced draft fan 101, and a detonation-resistant gas intake flame arrester 102 (also referred to as detonation-resistant gas intake flame arrester) connected to a gas path of the gas delivery induced draft fan 101; the gas pipeline of which the gas inlet end is connected with the methylene dichloride gas inlet is also provided with an oil gas pressure transmitter 103.
In this embodiment, specifically, the above-mentioned gas-gas heat recovery unit 200 includes a gas-gas heat recovery unit 201, the hot side air inlet end of the gas-gas heat recovery unit 201 is connected to the gas transmission induced draft fan 101, the hot side air outlet end of the gas-gas heat recovery unit 201 is connected to the air inlet end of the main condensation unit 300, the air outlet end of the main condensation unit 300 is connected to the cold side air inlet end of the gas-gas heat recovery unit 201 through a one-way valve, and the liquid outlet of the gas-gas heat recovery unit 201 is connected to the liquid inlet of the coalescer 307 (may also be referred to as a liquid collecting tank or a first coalescing separator tank).
In this embodiment, specifically, the main condensing unit 300 includes a gas path switching valve a301, a gas path switching valve B302, a main condenser a303, a main condenser B304, a check valve a305, a check valve B306, and a coalescer 307;
the gas path inlets of the gas path switching valve A301 and the gas path switching valve B302 are communicated with the hot side gas outlet end of the gas-gas heat regenerator 201; the gas path outlets (i.e., gas outlet ends) of the check valve A305 and the check valve B306 are connected with the cold side gas inlet end of the gas-gas regenerator 201; the liquid outlets of the main condenser A303 and the main condenser B304 are communicated with the coalescer 307; the coalescer 307 separates sewage and methylene dichloride and outputs/conveys the sewage and methylene dichloride to a user designated position;
The air channel outlet of the air channel switching valve A301 is communicated with the air inlet end of the main condenser A303, the air outlet end of the main condenser A303 is communicated with the air inlet end of the one-way valve A305, and the air outlet end of the one-way valve A305 is connected with the cold side air inlet end of the air-air regenerator 201;
the air passage outlet of the air passage switching valve B302 is communicated with the air inlet end of the main condenser B304; the air outlet end of the main condenser B304 is communicated with the air inlet end of the check valve B306, and the air outlet end of the check valve B306 is connected with the cold side air inlet end of the air-air heat regenerator 201.
As shown in fig. 1, one end of the cold carrier liquid inlet valve a703 and one end of the heat carrier liquid inlet valve a709 are connected to the carrier inlet of the main condenser a303, and one end of the cold carrier liquid outlet valve a705 and one end of the heat carrier liquid outlet valve a711 are connected to the carrier outlet of the main condenser a 303;
wherein one end of the cold carrier liquid inlet valve B704 and one end of the heat carrier liquid inlet valve B710 are both connected to the carrier inlet of the main condenser B304, and one end of the cold carrier liquid outlet valve B706 and one end of the heat carrier liquid outlet valve B712 are both connected to the carrier outlet of the main condenser B304;
the air conditioner is characterized in that when the main condenser is used for refrigerating, the carrier inlet/outlet of the air conditioner is the inlet/outlet of a refrigerating pipeline, and when the main condenser is used for heating/defrosting, the carrier inlet/outlet of the air conditioner is the inlet/outlet of a defrosting pipeline;
In this embodiment, specifically, as shown in fig. 1, the resin adsorption unit 400 includes an adsorption tank a401, an adsorption tank B402, an adsorption tank C403, an adsorption inlet valve a404, an adsorption inlet valve B405, an adsorption inlet valve C406, an adsorption outlet valve a407, an adsorption outlet valve B408, an adsorption outlet valve C409, an analysis inlet valve a410, an analysis inlet valve B411, an analysis inlet valve C412, a purge inlet valve a413, a purge inlet valve B414, a purge inlet valve C415, an analysis outlet valve a416, an analysis outlet valve B417, an analysis outlet valve C418, and an adsorption bypass valve 419;
the cold side air outlet end of the air-air regenerator 201 is communicated with one end of the adsorption bypass valve 419, one end of the adsorption inlet valve A404, one end of the adsorption inlet valve B405 and one end of the adsorption inlet valve C406; the other end of the adsorption bypass valve 419 communicates with the exhaust unit 500; the other end of the adsorption inlet valve A404 is communicated with the lower end of the adsorption tank A401, the other end of the adsorption inlet valve B405 is communicated with the lower end of the adsorption tank B402, and the other end of the adsorption inlet valve C406 is communicated with the lower end of the adsorption tank C403;
the upper end of the adsorption tank A401 is communicated with one end of an adsorption outlet valve A407, the upper end of the adsorption tank B402 is communicated with one end of an adsorption outlet valve B408, and the upper end of the adsorption tank C403 is communicated with one end of an adsorption outlet valve C409;
The other end of the adsorption-out valve a407, the other end of the adsorption-out valve B408, and the other end of the adsorption-out valve C409 are all communicated with the exhaust unit 500;
one end of the analysis inlet valve A410 is communicated with the upper end of the adsorption tank A401, one end of the analysis inlet valve B411 is communicated with the upper end of the adsorption tank B402, and one end of the analysis inlet valve C412 is communicated with the upper end of the adsorption tank C403; the other end of the analysis inlet valve A410, the other end of the analysis inlet valve B411 and the other end of the analysis inlet valve C412 are communicated with a desorption/analysis steam inlet;
one end of the purging inlet valve A413 is communicated with the upper end of the adsorption tank A401, one end of the purging inlet valve B414 is communicated with the upper end of the adsorption tank B402, and one end of the purging inlet valve C415 is communicated with the upper end of the adsorption tank C403; the other end of the purge inlet valve A413, the other end of the purge inlet valve B414 and the other end of the purge inlet valve C415 are communicated with a nitrogen inlet for desorption/purging;
one end of the analysis valve A416 is communicated with the lower end of the adsorption tank A401, one end of the analysis valve B417 is communicated with the lower end of the adsorption tank B402, and one end of the analysis valve C418 is communicated with the lower end of the adsorption tank C403;
the other end of the analysis outlet valve a416, the other end of the analysis outlet valve B417, and the other end of the analysis outlet valve C418 are all connected to the input end (intake end) of the multi-stage cooler 801 of the analysis cooling unit 800.
In this embodiment, for the adsorption of the dichloromethane waste gas configured with 3 adsorption tanks, the adsorption of the third tank in parallel can be performed by two-by-two desorption purge, or the desorption purge of 1 tank is performed by 1 tank for another 1 tank. Namely: and (3) alternately performing normal-temperature resin adsorption, high-temperature steam analysis and nitrogen purging cooling according to a set period through two adsorption and analysis or one adsorption and one analysis and three adsorption tanks for standby. The adsorption tank A, the adsorption tank B and the adsorption tank C in the temperature swing adsorption unit alternately perform normal temperature adsorption-high temperature steam analysis/desorption-nitrogen purging cooling modes (for example, the adsorption tank A and the adsorption tank B perform normal temperature adsorption, the adsorption tank C perform high temperature steam analysis and nitrogen purging cooling for standby, the adsorption tank B and the adsorption tank C perform normal temperature adsorption, the adsorption tank A perform high temperature steam analysis and nitrogen purging cooling for standby, the adsorption tank C and the adsorption tank A perform normal temperature adsorption, the adsorption tank B perform high temperature steam analysis and nitrogen purging cooling for standby, and the adsorption tank A and the adsorption tank B perform normal temperature adsorption, and the adsorption tank C perform high temperature steam analysis and nitrogen purging cooling for standby … …) to complete one adsorption cycle.
In the present embodiment, the above-described exhaust unit 500 includes an evacuation cylinder 501, a deflagration-resistant outlet flame arrester 502, a concentration detector 503; the concentration detector 503 is arranged in the middle of the tube body (such as the center of the tube body) of the emptying tube 501;
The intake port of the exhaust pipe 501 communicates with the other end of the adsorption bypass valve 419, the other end of the adsorption outlet valve a407, the other end of the adsorption outlet valve B408, and the other end of the adsorption outlet valve C409 through the deflagration-preventing outlet flame arrestor 502.
In the present embodiment, specifically, the above-described analytical cooling unit 800 includes a multistage cooler 801 and a coalescing separator tank 802 (may also be referred to as a second coalescing separator tank);
the cold source of the multistage cooler 801 is circulating cooling water or circulating chilled water; the air outlet end of the multistage cooler 801 is connected with the air inlet end of the deflagration-resistant air inlet flame arrester 102; the liquid outlet end of the multistage cooler 801 is communicated with the liquid inlet end of the coalescence-separation tank 802;
the coalescence-separation tank 802 separates dichloromethane and water and outputs the separated dichloromethane and water, or the separated condensate and sewage are transported to a user-designated location.
In this embodiment, specifically, the refrigeration unit 600 includes a refrigeration compressor 601, a water-cooled condenser 602, a subcooler 603, and a refrigeration throttling device 604 connected in sequence;
the other end of the refrigeration throttling device 604 is communicated with a refrigerant inlet of the intermediate heat exchanger 701, and a refrigerant outlet of the intermediate heat exchanger 701 is communicated with an input end of the refrigeration compressor 601;
The cold source of the water-cooled condenser 602 is circulating cooling water;
the heat-carrying outlet of the subcooler 603 is connected to the inlet of the heat-carrying pump 708 (also referred to as heat-carrying agent inlet), and the heat-carrying inlet of the subcooler 603 is connected to the other end of the heat-carrying liquid outlet valve a711 and the other end of the heat-carrying liquid outlet valve B712.
Taking the condensation adsorption recovery system for dichloromethane gas provided in the above embodiment as an example, the relevant working principle/working procedure is illustrated:
in the gas delivery unit 100: conveying dichloromethane gas to a next-ring gas-saving heat regeneration unit through a gas-conveying induced draft fan;
in the gas-gas heat recovery unit 200: the primary pre-cooling treatment is carried out on the methylene dichloride gas input by the gas transmission unit through the gas regenerator 201, and the method specifically comprises the following steps: preliminary precooling treatment is carried out on methylene dichloride gas input from a hot side air inlet end of the gas regenerator 201; outputting the gas subjected to preliminary precooling treatment from a hot side air outlet end of the gas-gas regenerator 201 to a main condensing unit for multistage condensation and liquid separation; the cold recovery is carried out on the low-concentration dichloromethane gas which is input from the cold side air inlet end of the gas-gas heat regenerator 201 and is not precipitated after multi-stage condensation liquid separation, so that the temperature of the low-concentration dichloromethane gas is raised to 20-25 ℃, and the low-concentration dichloromethane gas is output from the cold side air outlet end of the gas-gas heat regenerator 201 to a resin adsorption unit for resin adsorption and/or discharge;
In the main condensing unit 300: carrying out multistage condensation and analysis on the gas subjected to preliminary precooling treatment to obtain most of methylene dichloride condensate, returning and outputting the low-concentration methylene dichloride gas which is not separated out to a gas recovery unit through an outlet end/gas path outlet of a main condenser, carrying out cold recovery and temperature rise, and then carrying out resin adsorption and/or discharge; the separated dichloromethane condensate enters a coalescer from a liquid outlet of a main condenser, and a large amount of dichloromethane liquid and a small amount of water are separated through standing, coalescing and separation of the coalescer for collection/discharge;
in the resin adsorption unit 400: the method comprises the steps of alternately performing normal-temperature resin adsorption, high-temperature steam analysis and nitrogen purging cooling on dichloromethane gas output in the previous step according to a set period through an adsorption system with one adsorption-analysis-standby or two adsorption-analysis-three adsorption tanks; outputting the gas after normal temperature adsorption to the next link for discharge (namely, absorbing/adsorbing the dichloromethane gas output by the previous link through an adsorption tank, and outputting the gas after absorbing/adsorbing to the next link for discharge);
in the analytical cooling unit 800: the gas-liquid mixture output by high-temperature steam analysis and nitrogen purging and cooling in the resin adsorption unit 400 is subjected to cooling treatment by a multi-stage cooler, the gas output after the cooling treatment is returned to the front end of a gas delivery induced draft fan to be subjected to primary pre-cooling, multi-stage condensation liquid separation, temperature-variable resin adsorption and monitoring discharge treatment processes, and the liquid output after the cooling treatment is subjected to standing, coalescence and separation by a coalescence-separation tank to obtain a large amount of condensed water and a small amount of dichloromethane liquid which are respectively discharged/collected;
Based on the structures and the constructions of the carrier unit 700, the refrigeration unit 600 and the main condensation unit 300 provided in this embodiment, the refrigeration unit can realize indirect condensation on the main condenser through the secondary refrigerant, and can also realize indirect defrosting on the main condenser through the heat carrier: when the main condensers of the main condensing unit 300 are in the condensing mode, refrigerating the refrigerant in the refrigerant refrigerating cycle by the freon refrigerating cycle of the refrigerating unit, thereby providing a cold source for multistage condensation of each main condenser, and realizing indirect condensation of the main condensers of the main condensing unit by the freon refrigerating cycle of the refrigerating unit; when the main condensers of the main condensing units 300 are in the defrosting mode, the heat carrier in the carrier defrosting cycle is heated through the Freon refrigerating cycle of the refrigerating unit, so that a heat source is provided for defrosting of each main condenser, and indirect defrosting of the Freon refrigerating cycle of the refrigerating unit to the main condensers of the main condensing units is realized; wherein: the cold source in the condensing mode of the main condensing unit 300 is provided by the coolant in the carrier refrigeration cycle of the carrier unit 700 and the heat source in the defrosting mode of the main condensing unit 300 is provided by the heat carrier in the carrier defrosting cycle of the carrier unit 700.
In the exhaust unit 500: and (5) performing concentration monitoring and discharging on the gas output in the previous step.
In the refrigeration unit 600, specifically: the freon refrigeration cycle provides refrigeration to the intermediate heat exchanger 701 and heat to the subcooler 603: after passing through the refrigeration compressor 601, the water-cooled condenser 602 and the subcooler 603 in sequence, the freon refrigerant is input into the intermediate heat exchanger 701 through the refrigeration throttling device 604, is output from the intermediate heat exchanger 701 and then enters the refrigeration compressor 601 to form freon refrigeration cycle; in the freon refrigeration cycle, the water-cooled condenser 602 and the subcooler 603 are on the high temperature side (i.e., the condensing side, which is an exothermic process of changing the gas state into the liquid state), and the intermediate heat exchanger 701 is on the low temperature side (i.e., the evaporating side, which is an endothermic process of changing the liquid state into the gas state).
Taking main condenser a303 as an example: the corresponding heat-carrying liquid inlet valve A709 and the heat-carrying liquid outlet valve A711 are closed, the corresponding cold-carrying liquid inlet valve A703 and the cold-carrying liquid outlet valve A705 are opened, and the main condenser A303 is in a condensing mode. Taking main condenser B304 as an example: the corresponding heat-carrying liquid inlet valve B710 and the heat-carrying liquid outlet valve B712 are closed, the corresponding cold-carrying liquid inlet valve B704 and the cold-carrying liquid outlet valve B706 are opened, and the main condenser B304 is in a condensing mode.
For the main condenser in a condensing mode, corresponding to the main condenser, with the heat-carrying liquid inlet valve and the heat-carrying liquid outlet valve closed and the cold-carrying liquid inlet valve and the cold-carrying liquid outlet valve opened, the carrier refrigeration cycle is as follows: the coolant is output from the cold-carrying outlet of the intermediate heat exchanger 701 after heat exchange with the freon refrigeration cycle, is input to the main condenser (input from the cold-carrying inlet of the main condenser to supply cold/cold source to the main condenser) via the cold-carrying pump 702 and the cold-carrying liquid inlet valve corresponding thereto, is output from the main condenser (output from the cold-carrying outlet of the main condenser), and is input to the intermediate heat exchanger 701 (input from the cold-carrying inlet of the intermediate heat exchanger 701) via the cold-carrying liquid outlet valve corresponding thereto to form the carrier refrigeration cycle.
Taking main condenser a303 as an example: and opening the corresponding heat-carrying liquid inlet valve A709 and the heat-carrying liquid outlet valve A711, closing the corresponding cold-carrying liquid inlet valve A703 and the cold-carrying liquid outlet valve A705, and putting the main condenser A303 in a defrosting mode. Taking main condenser B304 as an example: and opening the corresponding heat-carrying liquid inlet valve B710 and the heat-carrying liquid outlet valve B712, closing the corresponding cold-carrying liquid inlet valve B704 and the cold-carrying liquid outlet valve B706, and putting the main condenser B304 into a defrosting mode.
For the main condensers in defrosting mode, which are corresponding to the main condensers and are opened, and corresponding to the main condensers and are closed, the carrier defrosting cycle is as follows: the heat carrier is output from the heat carrier outlet of the subcooler 603 after exchanging heat with the freon refrigeration cycle in the subcooler 603, is input into the main condenser (input from the carrier inlet of the main condenser to provide heat/heat source for the main condenser) through the heat carrier pump 708 and the heat carrier liquid inlet valve corresponding thereto, and is further output from the main condenser (output from the carrier outlet of the main condenser) and is input into the subcooler 603 (input from the heat carrier inlet of the subcooler 603) through the heat carrier liquid outlet valve corresponding thereto to form the carrier defrosting cycle.
The Freon refrigerating system is mostly welded because of being unable to leak, and equipment maintenance and replacement are difficult. The devices in the carrier unit/system of the present invention are flange-connected and the carrier (including coolant and heat carrier) is conveniently filled. Therefore, the indirect condensation and indirect defrosting can be realized based on the structure and the structure provided by the invention, not only can the corrosion/pollution possibly caused by the aqueous methylene dichloride solution to the heat exchanger (comprising the intermediate heat exchanger 701 and the subcooler 603 in the Freon refrigeration cycle) in the refrigeration unit Freon refrigeration cycle be effectively avoided, but also the risk of direct pollution caused by the aqueous methylene dichloride solution to the Freon refrigerant can be greatly reduced, the risk of leakage of the Freon refrigeration system can be effectively avoided/relieved, and the possibility of repair welding fire operation on the site of the refrigeration unit Freon refrigeration cycle due to corrosion, pollution, leakage and the like can be well avoided/reduced.
Wherein the normal temperature resin adsorption in the resin adsorption unit 400 includes: after the cold recovery temperature of the dichloromethane gas output by the main condensing unit 300 is raised, the dichloromethane gas enters a corresponding adsorption tank through a corresponding adsorption inlet valve, is subjected to strong adsorption of the adsorption resin at the temperature of about 20-25 ℃ and is output to a subsequent process through a corresponding adsorption outlet valve.
Wherein the high temperature steam analysis in the resin adsorption unit 400 includes: and (3) for the adsorption tank switched to the analysis mode, closing the corresponding adsorption inlet valve and the adsorption outlet valve, opening the corresponding desorption inlet valve and the desorption outlet valve, uniformly spraying high-temperature steam (with the temperature of 110-130 ℃ and preferably 120 ℃) from the top of the adsorption tank onto the adsorption resin through a steam distributor, and enabling the high-temperature steam to be in direct and full contact with the adsorption resin bed layer to carry out analysis regeneration of the adsorption resin, wherein the analysis period is generally 1-2 hours and can be completed.
Wherein the nitrogen purge cooling in the resin adsorption unit 400 includes: and (3) closing the corresponding desorption inlet valve of the adsorption tank for completing the desorption of the steam, opening the corresponding purging inlet valve of the adsorption tank, and purging the adsorption resin bed layer by injecting nitrogen at normal temperature or after precooling from the top of the adsorption tank, so as to purge residual water vapor in the adsorption resin bed layer, and cooling the adsorption resin bed layer until the temperature in the adsorption tank is reduced to the normal temperature, thereby completing the nitrogen purging work.
The multistage condensation provided by the main condenser in the invention is a process for reducing the temperature below the boiling point of dichloromethane by utilizing the relationship that the saturated vapor pressure of dichloromethane is reduced along with the reduction of the temperature, so that the dichloromethane is changed from the gas state to the liquid state, and has good recovery effect on high-concentration dichloromethane waste gas. Experiments prove that: the concentration of the dichloromethane waste gas which is discharged by the external process device and is about 13 ℃ is up to 468.3g/m 3 (about 35% of saturation concentration), the concentration of the gas discharged after multi-stage condensation to about-65 ℃ by the main condenser of the invention is about 10.2g/m 3 The recovery efficiency can reach more than 97 percent.
In general, in the invention, dichloromethane gas is sequentially conveyed by a conveying fan (namely a gas conveying induced draft fan) of a gas conveying unit 100, is subjected to primary pre-cooling treatment by a gas backheating unit 200, then enters a main condensing unit 300 for multi-stage condensation analysis liquid to separate out most dichloromethane condensate liquid, and the low-concentration dichloromethane gas/tail gas which is not separated out returns to the cold side inlet end of a gas backheating unit 201 to enter the gas backheating unit for cold energy recovery, so that the temperature of the dichloromethane gas is returned to 20-25 ℃, and is output to a resin adsorption unit from the cold side outlet end of the gas backheating unit 201; the low-concentration methylene dichloride gas is adsorbed and enriched in the resin adsorption unit 400 (the normal temperature is 20-25 ℃ and the normal pressure is 5000-6000 Pa), and the waste gas reaching the standard is discharged after being adsorbed through the exhaust unit 500 reaching the standard, so that the condensation adsorption recovery flow of the methylene dichloride gas is completed.
Wherein the cold source in the condensing mode of the main condensing unit 300 is provided by the carrier refrigeration cycle (also referred to as a carrier refrigeration cycle) of the carrier unit 700, and the heat source in the defrosting mode of the main condensing unit 300 is provided by the carrier defrosting cycle (also referred to as a carrier defrosting cycle) of the carrier unit 700. Both the cold source of the carrier refrigeration cycle of the carrier unit 700 and the heat source of the carrier defrosting cycle are provided by the freon refrigeration cycle (also referred to as a freon refrigeration cycle system) of the refrigeration unit 600.
The methylene dichloride aqueous solution subjected to high-temperature steam analysis and nitrogen purging after adsorption enrichment and temperature reduction by the resin adsorption unit 400 is cooled, kept stand, coalesced and separated in the analysis cooling unit 800 to obtain a large amount of condensed water and a small amount of methylene dichloride (the relative density of the methylene dichloride is 1.33 (water=1), the solubility in water (20 ℃) is 10-20 g/L, the solubility in water is lower and the relative density with water is larger); the methylene dichloride condensate separated out by the multi-stage condensation analysis liquid of the main condensation unit 300 is also subjected to caching, standing, coalescence and separation to obtain a large amount of methylene dichloride and a small amount of sewage; the treatment of the dichloromethane liquid solvent was completed.
In this example, the superficial flow rate of each of the above-mentioned adsorption tanks is 0.05m/s to 0.25m/s, and the gas residence time (i.e., the time for the gas to pass through the adsorbent bed/the adsorbent resin bed) is 3s or more.
Taking a certain adsorption tank as an example, the related working principles/working procedures of adsorption of resin at normal temperature, high-temperature steam analysis and nitrogen purging and cooling are illustrated as follows: the DLJ high polymer adsorption resin is adopted in the adsorption tank as an adsorbent to perform normal-temperature adsorption on dichloromethane in waste gas (at the moment, an adsorption inlet valve and an adsorption outlet valve corresponding to the adsorption tank are opened, an analysis inlet valve and a purging inlet valve and an analysis outlet valve corresponding to the adsorption tank are closed), the high polymer adsorption resin is desorbed and regenerated by high-temperature steam after one period of normal-temperature adsorption is completed, and dichloromethane steam generated by desorption and regeneration can be condensed, separated and recycled. The specific adsorption flow is as follows: the low concentration dichloromethane waste gas discharged from the main condenser is cooled by a gas regenerator and the temperature is raised, then enters the adsorption tank from the bottom to be uniformly contacted with a high polymer adsorption resin bed layer, the adsorption state is normal temperature 20-25 ℃ and normal pressure 5000-6000 Pa (the temperature and pressure of the gas in the adsorption tank in the adsorption state), the standard waste gas fully adsorbed by the resin is discharged from the high altitude of the emptying cylinder, wherein the concentration of the dichloromethane in the standard waste gas discharged from the high altitude is not higher than 54.8mg/m 3 The removal rate of the dichloromethane of the resin adsorption unit can reach more than 99 percent.
After the normal temperature resin is adsorbed for a certain period, closing an adsorption inlet valve and an adsorption outlet valve corresponding to the adsorption tank, simultaneously opening an analysis inlet valve and an analysis valve corresponding to the adsorption tank, entering a high temperature steam desorption/analysis mode, and carrying out desorption/analysis regeneration on the high polymer adsorption resin by using high temperature low pressure steam of 0.1-0.2 MPa: the high-temperature low-pressure steam is uniformly sprayed onto the adsorption resin bed layer from the top of the adsorption tank through a steam distributor (namely a steam flow equalizer, wherein a certain spraying height is reserved between the steam distributor and the top end of the adsorption resin bed layer), the high-temperature low-pressure steam is introduced into the adsorption resin bed layer for displacement desorption (namely the high-temperature steam is in direct full contact with the adsorption resin bed layer for desorption and regeneration of the adsorption resin), in the embodiment, the desorption state is that the high temperature is adjustable at 110-130 ℃, the temperature of the high-temperature steam in the steam desorption/desorption process is adjustable, the desorption time is preferably 120 ℃, and the displacement desorption is adjustable for 1-2 h.
The temperature of the adsorption resin bed layer after displacement desorption is higher, the desorption inlet valve corresponding to the adsorption tank is closed, the purging inlet valve corresponding to the adsorption tank is opened, nitrogen gas after normal temperature or precooling is introduced into the adsorption resin bed layer, and the purging steam is purged until the adsorption resin bed layer is cooled to the normal temperature, so that nitrogen purging cooling work is completed, and the adsorption tank enters a standby state to wait for the next adsorption period to be adsorbed again. The gas-liquid mixture which is output by high-temperature steam analysis and nitrogen purging and cooling in the adsorption tank is output to a multi-stage cooler for cooling and other related treatments through an analysis outlet valve corresponding to the adsorption tank.
The carrier refrigeration cycle described herein may also be referred to as a coolant refrigeration cycle, or a carrier refrigeration cycle, or a coolant cycle. The vehicle defrost cycle described herein may also be referred to as a vehicle defrost cycle, and may also be referred to as a vehicle heating cycle, or a vehicle heat-carrying cycle, or a vehicle cycle. The carrier refrigeration cycle system described herein may also be referred to as a carrier refrigeration/refrigeration cycle system, or a coolant cycle system. The vehicle defrost cycle system described herein may also be referred to as a vehicle heat-carrying/heating cycle system, or a heat-carrying cycle system. The refrigeration capacity associated with Wen Zhongzai, carrier defrost and freon refrigeration cycles may also be referred to as a cold source, and the heat associated with carrier refrigeration cycles, carrier defrost and freon refrigeration cycles may also be referred to as a heat source.
The inlet end may also be referred to herein as an end or inlet end, or simply as an inlet or inlet end. The outlet end may also be referred to herein as the other end, or simply as the outlet or outlet end. The methylene chloride gas described herein may also be referred to as a methylene chloride off-gas, or a methylene chloride-containing off-gas/body. The desorption inlet valve described herein may also be referred to as a desorption inlet valve or a vapor inlet valve. The desorption outlet valve described herein may also be referred to as a desorption valve or a vapor outlet valve, or a desorption/desorption purge outlet valve. The defrosting lines described herein may also be referred to as heating lines. The inlet/outlet of the air path may also be referred to herein simply as the inlet/outlet or inlet/outlet end. The hot side gas path inlet/outlet may also be referred to herein as a high Wen Qilu inlet/outlet or a high temperature inlet/outlet. The gas path switching valve described herein may also be referred to as an intake switching valve. The "/" herein indicates or.
The term "a" as used herein may also be referred to as "first". The term "B" as used herein may also be referred to as "second". The term "C" as used herein may also be referred to as "third". The "adsorption inlet valve" may be an adsorption tank, an adsorption inlet valve, an adsorption outlet valve, a desorption inlet valve, a purge inlet valve, a desorption outlet valve, or the like.
The above embodiments do not limit the present invention, and various changes and modifications can be made by the related workers within the scope of not departing from the technical spirit of the present invention, all of which fall within the scope of protection of the present invention.
Claims (12)
1. A condensation adsorption recovery system for methylene chloride gas, characterized in that: the device comprises a gas transmission unit (100), a gas-gas heat recovery unit (200) connected with a gas path of the gas transmission unit (100), a main condensing unit (300) connected with the gas path of the gas-gas heat recovery unit (200), a carrier unit (700) connected with the main condensing unit (300), a refrigerating unit (600) connected with the carrier unit (700), a resin adsorption unit (400) connected with the gas-gas heat recovery unit (200), a resolution cooling unit (800) connected with the resin adsorption unit (400) and an exhaust unit (500) connected with the resin adsorption unit (400);
the resin adsorption unit (400) is provided with an adsorption bypass valve (419); an air inlet end of the adsorption bypass valve (419) is connected with the main condensing unit (300), and an air outlet end of the adsorption bypass valve is connected with the exhaust unit (500);
The system is also provided with a carrier refrigeration cycle system and a carrier defrosting cycle system; the refrigerating unit (600) provides cold for the refrigerating medium in the carrier refrigerating cycle system and provides heat for the heat carrier in the carrier defrosting cycle system; the vehicle refrigeration cycle provides cold to the main condensing unit (300) and the vehicle defrost cycle provides heat to the main condensing unit (300).
2. The condensation adsorption recovery system for methylene chloride gas according to claim 1, wherein: the carrier unit (700) comprises an intermediate heat exchanger (701), a carrier cooling pump (702), a carrier cooling liquid inlet valve A (703), a carrier cooling liquid inlet valve B (704), a carrier cooling liquid outlet valve A (705), a carrier cooling liquid outlet valve B (706), a carrier cooling expansion tank (707), a carrier heat pump (708), a carrier heating liquid inlet valve A (709), a carrier heating liquid inlet valve B (710), a carrier heating liquid outlet valve A (711), a carrier heating liquid outlet valve B (712) and a carrier heating expansion tank (713);
the carrier refrigeration cycle system comprises: a cold-carrying liquid outlet valve A (705) and a cold-carrying liquid outlet valve B (706) which are arranged in parallel, an intermediate heat exchanger (701), a cold-carrying pump (702), a cold-carrying liquid inlet valve A (703) and a cold-carrying liquid inlet valve B (704) which are arranged in parallel;
the vehicle defrosting circulation system comprises the following components connected in sequence: a heat-carrying liquid outlet valve A (711) and a heat-carrying liquid outlet valve B (712) which are arranged in parallel, a subcooler (603), a heat-carrying pump (708), and a heat-carrying liquid inlet valve A (709) and a heat-carrying liquid inlet valve B (710) which are arranged in parallel.
3. The condensation adsorption recovery system for methylene chloride gas according to claim 2, wherein:
the outlet cold liquid of the cold carrying pump (702) can be sent to the carrier inlet of the main condenser A (303) through the cold carrying liquid inlet valve A (703), the carrier outlet of the main condenser A (303) is connected with the cold carrying liquid outlet valve A (705), the other end of the cold carrying liquid outlet valve A (705) is connected with the cold carrying inlet of the intermediate heat exchanger (701), and the cold carrying outlet of the intermediate heat exchanger (701) is connected with the inlet of the cold carrying pump (702);
the outlet cold liquid of the cold-carrying pump (702) can be sent to the carrier inlet of the main condenser B (304) through the cold-carrying liquid inlet valve B (704), the carrier outlet of the main condenser B (304) is connected with the cold-carrying liquid outlet valve B (706), the other end of the cold-carrying liquid outlet valve B (706) is connected with the cold-carrying inlet of the intermediate heat exchanger (701), and the cold-carrying outlet of the intermediate heat exchanger (701) is connected with the inlet of the cold-carrying pump (702);
the outlet hot liquid of the heat-carrying pump (708) can be sent to the carrier inlet of the main condenser A (303) through the heat-carrying liquid inlet valve A (709), the carrier outlet of the main condenser A (303) is connected with the heat-carrying liquid outlet valve A (711), the other end of the heat-carrying liquid outlet valve A (711) is connected with the heat-carrying inlet of the subcooler (603), and the heat-carrying outlet of the subcooler (603) is connected with the inlet of the heat-carrying pump (708);
The outlet hot liquid of the heat-carrying pump (708) can be sent into the carrier inlet of the main condenser B (304) through the heat-carrying liquid inlet valve B (710), the carrier outlet of the main condenser B (304) is connected with the heat-carrying liquid outlet valve B (712), the other end of the heat-carrying liquid outlet valve B (712) is connected with the heat-carrying inlet of the subcooler (603), and the heat-carrying outlet of the subcooler (603) is connected with the inlet of the heat-carrying pump (708).
4. The condensation adsorption recovery system for methylene chloride gas according to claim 1, wherein:
a DLJ type high polymer adsorption resin is adopted as an adsorbent in the resin adsorption unit (400); and/or
The devices in the carrier unit (700) are connected by adopting flanges; and/or
The heat carrier and the secondary refrigerant are propanol; and/or
The bottom of each adsorption tank in the resin adsorption unit (400) is provided with a grating plate, and a first filter screen layer, a second steel wire screen layer and a third steel wire screen layer are sequentially arranged on the grating plate from bottom to top; wherein, a first layer of porcelain balls are filled between the first filtering silk screen layer and the second steel wire mesh layer; resin adsorbents are filled between the second steel wire mesh layer and the third steel wire mesh layer; a second layer of porcelain balls are paved on the third steel wire mesh layer; and/or
The first filter screen layer was a 50 mesh 254SMO steel filter screen.
5. The condensation adsorption recovery system for methylene chloride gas according to claim 1, wherein: the gas transmission unit (100) comprises a gas transmission induced draft fan (101) and a deflagration-resistant gas inlet flame arrester (102) connected with a gas path of the gas transmission induced draft fan (101); an oil gas pressure transmitter (103) is also arranged on a gas pipeline of which the gas inlet end of the gas inlet flame arrester (102) is connected with the methylene dichloride gas inlet; and/or
Spherical adsorption resin with the diameter of 0.3-1.2 mm is adopted as an adsorbent in the adsorption tanks of the resin adsorption unit (400).
6. The condensation adsorption recovery system for methylene chloride gas according to claim 1, wherein: the gas-gas heat recovery unit (200) comprises a gas-gas heat recovery unit (201), a hot side air inlet end of the gas-gas heat recovery unit (201) is connected with a gas transmission induced draft fan (101), a hot side air outlet end of the gas-gas heat recovery unit (201) is connected with an air inlet end of a main condensing unit (300), an air outlet end of the main condensing unit (300) is connected with a cold side air inlet end of the gas-gas heat recovery unit (201), and a liquid outlet of the gas-gas heat recovery unit (201) is connected with a liquid inlet of a coalescer (307).
7. The condensation adsorption recovery system for methylene chloride gas according to claim 6, wherein: the main condensation unit (300) comprises an air passage switching valve A (301), an air passage switching valve B (302), a main condenser A (303), a main condenser B (304), a one-way valve A (305), a one-way valve B (306) and a coalescer (307);
The gas channel inlets of the gas channel switching valve A (301) and the gas channel switching valve B (302) are communicated with the hot side gas outlet end of the gas-gas heat regenerator (201); the liquid outlets of the main condenser A (303) and the main condenser B (304) are communicated with the coalescer (307); the coalescer (307) separates out sewage and methylene dichloride and outputs the sewage and methylene dichloride respectively;
the air channel outlet of the air channel switching valve A (301) is communicated with the air inlet end of the main condenser A (303), the air outlet end of the main condenser A (303) is communicated with the air inlet end of the one-way valve A (305), and the air outlet end of the one-way valve A (305) is connected with the cold side air inlet end of the air-air regenerator (201);
the air passage outlet of the air passage switching valve B (302) is communicated with the air inlet end of the main condenser B (304); the air outlet end of the main condenser B (304) is communicated with the air inlet end of the one-way valve B (306), and the air outlet end of the one-way valve B (306) is connected with the cold side air inlet end of the air-air heat regenerator (201).
8. The condensation adsorption recovery system for methylene chloride gas according to claim 7, wherein:
wherein one end of the cold-carrying liquid inlet valve A (703) and one end of the heat-carrying liquid inlet valve A (709) are connected with the carrier inlet of the main condenser A (303), and one end of the cold-carrying liquid outlet valve A (705) and one end of the heat-carrying liquid outlet valve A (711) are connected with the carrier outlet of the main condenser A (303);
Wherein one end of the cold-carrying liquid inlet valve B (704) and one end of the heat-carrying liquid inlet valve B (710) are connected with the carrier inlet of the main condenser B (304), and one end of the cold-carrying liquid outlet valve B (706) and one end of the heat-carrying liquid outlet valve B (712) are connected with the carrier outlet of the main condenser B (304).
9. The condensation adsorption recovery system for methylene chloride gas according to claim 6, wherein: the resin adsorption unit (400) comprises an adsorption tank A (401), an adsorption tank B (402), an adsorption tank C (403), an adsorption inlet valve A (404), an adsorption inlet valve B (405), an adsorption inlet valve C (406), an adsorption outlet valve A (407), an adsorption outlet valve B (408), an adsorption outlet valve C (409), an analysis inlet valve A (410), an analysis inlet valve B (411), an analysis inlet valve C (412), a purge inlet valve A (413), a purge inlet valve B (414), a purge inlet valve C (415), an analysis outlet valve A (416), an analysis outlet valve B (417), an analysis outlet valve C (418) and an adsorption bypass valve (419);
the cold side air outlet end of the air-air heat regenerator (201) is communicated with one end of the adsorption bypass valve (419), one end of the adsorption inlet valve A (404), one end of the adsorption inlet valve B (405) and one end of the adsorption inlet valve C (406); the other end of the adsorption bypass valve (419) is communicated with the exhaust unit (500); the other end of the adsorption inlet valve A (404) is communicated with the lower end of the adsorption tank A (401), the other end of the adsorption inlet valve B (405) is communicated with the lower end of the adsorption tank B (402), and the other end of the adsorption inlet valve C (406) is communicated with the lower end of the adsorption tank C (403);
The upper end of the adsorption tank A (401) is communicated with one end of an adsorption outlet valve A (407), the upper end of the adsorption tank B (402) is communicated with one end of an adsorption outlet valve B (408), and the upper end of the adsorption tank C (403) is communicated with one end of an adsorption outlet valve C (409);
the other end of the adsorption-out valve A (407), the other end of the adsorption-out valve B (408) and the other end of the adsorption-out valve C (409) are communicated with the exhaust unit (500);
one end of the analysis inlet valve A (410) is communicated with the upper end of the adsorption tank A (401), one end of the analysis inlet valve B (411) is communicated with the upper end of the adsorption tank B (402), and one end of the analysis inlet valve C (412) is communicated with the upper end of the adsorption tank C (403); the other end of the analysis inlet valve A (410), the other end of the analysis inlet valve B (411) and the other end of the analysis inlet valve C (412) are communicated with a desorption/analysis steam inlet;
one end of the purging inlet valve A (413) is communicated with the upper end of the adsorption tank A (401), one end of the purging inlet valve B (414) is communicated with the upper end of the adsorption tank B (402), and one end of the purging inlet valve C (415) is communicated with the upper end of the adsorption tank C (403); the other end of the purge inlet valve A (413), the other end of the purge inlet valve B (414) and the other end of the purge inlet valve C (415) are communicated with a nitrogen inlet for desorption/purging;
One end of the analysis valve A (416) is communicated with the lower end of the adsorption tank A (401), one end of the analysis valve B (417) is communicated with the lower end of the adsorption tank B (402), and one end of the analysis valve C (418) is communicated with the lower end of the adsorption tank C (403);
the other end of the analysis outlet valve A (416), the other end of the analysis outlet valve B (417) and the other end of the analysis outlet valve C (418) are communicated with the input end of the multistage cooler (801) of the analysis cooling unit (800).
10. The condensation adsorption recovery system for methylene chloride gas according to claim 9, wherein:
the exhaust unit (500) comprises an exhaust cylinder (501), a deflagration-resistant outlet flame arrester (502) and a concentration detector (503); the concentration detector (503) is arranged in the middle of the tube body of the emptying tube (501);
an air inlet of the exhaust pipe (501) is communicated with the other end of the adsorption bypass valve (419), the other end of the adsorption outlet valve A (407), the other end of the adsorption outlet valve B (408) and the other end of the adsorption outlet valve C (409) through a deflagration-resistant outlet flame arrester (502).
11. The condensation adsorption recovery system for methylene chloride gas according to claim 5, wherein:
the analytical cooling unit (800) comprises a multistage cooler (801) and a coalescing separator tank (802);
The air outlet end of the multistage cooler (801) is connected with the air inlet end of the deflagration-resistant air inlet flame arrester (102); the liquid outlet end of the multistage cooler (801) is communicated with the liquid inlet end of the coalescence-separation tank (802);
the coalescence-separation tank (802) is used for separating dichloromethane and water and then outputting the separated dichloromethane and water.
12. The condensation adsorption recovery system for methylene chloride gas according to claim 1, wherein: the refrigeration unit (600) comprises a refrigeration compressor (601), a water-cooled condenser (602), a subcooler (603) and a refrigeration throttling device (604) which are connected in sequence;
the other end of the refrigeration throttling device (604) is communicated with a refrigerant inlet of the intermediate heat exchanger (701), and a refrigerant outlet of the intermediate heat exchanger (701) is communicated with an input end of a refrigeration compressor (601);
the heat-carrying outlet of the subcooler (603) is communicated with the inlet of the heat-carrying pump (708), and the heat-carrying inlet of the subcooler (603) is communicated with the other end of the heat-carrying liquid outlet valve A (711) and the other end of the heat-carrying liquid outlet valve B (712).
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