CN117619087A - Condensing adsorption recovery system for benzene-containing gas - Google Patents
Condensing adsorption recovery system for benzene-containing gas Download PDFInfo
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- CN117619087A CN117619087A CN202311687603.9A CN202311687603A CN117619087A CN 117619087 A CN117619087 A CN 117619087A CN 202311687603 A CN202311687603 A CN 202311687603A CN 117619087 A CN117619087 A CN 117619087A
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- 238000001179 sorption measurement Methods 0.000 title claims abstract description 376
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 title claims abstract description 259
- 238000011084 recovery Methods 0.000 title claims abstract description 62
- 238000003795 desorption Methods 0.000 claims abstract description 110
- 238000009833 condensation Methods 0.000 claims abstract description 49
- 230000005494 condensation Effects 0.000 claims abstract description 49
- 230000005540 biological transmission Effects 0.000 claims abstract description 29
- 239000011347 resin Substances 0.000 claims abstract description 26
- 229920005989 resin Polymers 0.000 claims abstract description 26
- 239000007788 liquid Substances 0.000 claims abstract description 24
- 238000001816 cooling Methods 0.000 claims abstract description 20
- 239000003463 adsorbent Substances 0.000 claims abstract description 17
- 230000006835 compression Effects 0.000 claims abstract description 9
- 238000007906 compression Methods 0.000 claims abstract description 9
- 239000007789 gas Substances 0.000 claims description 128
- 238000010926 purge Methods 0.000 claims description 50
- 238000005057 refrigeration Methods 0.000 claims description 32
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 32
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 29
- 229910052757 nitrogen Inorganic materials 0.000 claims description 15
- 239000003507 refrigerant Substances 0.000 claims description 10
- 239000000498 cooling water Substances 0.000 claims description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 15
- 239000002912 waste gas Substances 0.000 description 9
- 238000000926 separation method Methods 0.000 description 7
- 208000028659 discharge Diseases 0.000 description 6
- 238000000034 method Methods 0.000 description 6
- 239000010865 sewage Substances 0.000 description 4
- 239000002910 solid waste Substances 0.000 description 4
- 238000010257 thawing Methods 0.000 description 4
- 241000219095 Vitis Species 0.000 description 3
- 235000009754 Vitis X bourquina Nutrition 0.000 description 3
- 235000012333 Vitis X labruscana Nutrition 0.000 description 3
- 235000014787 Vitis vinifera Nutrition 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 238000011049 filling Methods 0.000 description 3
- 238000002844 melting Methods 0.000 description 3
- 230000008018 melting Effects 0.000 description 3
- 239000004005 microsphere Substances 0.000 description 3
- 238000004064 recycling Methods 0.000 description 3
- XPDWGBQVDMORPB-UHFFFAOYSA-N Fluoroform Chemical compound FC(F)F XPDWGBQVDMORPB-UHFFFAOYSA-N 0.000 description 2
- VEFXTGTZJOWDOF-UHFFFAOYSA-N benzene;hydrate Chemical compound O.C1=CC=CC=C1 VEFXTGTZJOWDOF-UHFFFAOYSA-N 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 229920000642 polymer Polymers 0.000 description 2
- 230000002265 prevention Effects 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- 238000010408 sweeping Methods 0.000 description 2
- LVGUZGTVOIAKKC-UHFFFAOYSA-N 1,1,1,2-tetrafluoroethane Chemical compound FCC(F)(F)F LVGUZGTVOIAKKC-UHFFFAOYSA-N 0.000 description 1
- UJPMYEOUBPIPHQ-UHFFFAOYSA-N 1,1,1-trifluoroethane Chemical compound CC(F)(F)F UJPMYEOUBPIPHQ-UHFFFAOYSA-N 0.000 description 1
- YCKRFDGAMUMZLT-UHFFFAOYSA-N Fluorine atom Chemical compound [F] YCKRFDGAMUMZLT-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000002457 bidirectional effect Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000005474 detonation Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 229910052731 fluorine Inorganic materials 0.000 description 1
- 239000011737 fluorine Substances 0.000 description 1
- 239000002920 hazardous waste Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- GTLACDSXYULKMZ-UHFFFAOYSA-N pentafluoroethane Chemical compound FC(F)C(F)(F)F GTLACDSXYULKMZ-UHFFFAOYSA-N 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 238000002336 sorption--desorption measurement Methods 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 239000012855 volatile organic compound Substances 0.000 description 1
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- Separation Of Gases By Adsorption (AREA)
Abstract
The invention discloses a condensation adsorption recovery system for benzene-containing gas, which comprises a gas transmission unit, a condensation recovery unit connected with a gas transmission unit gas circuit, a compression condensation unit connected with a condensation recovery unit refrigerating pipeline, a temperature swing adsorption unit connected with the condensation recovery unit gas circuit, a condensate cooling recovery unit connected with a temperature swing adsorption unit liquid circuit, and an evacuation unit communicated with the temperature swing adsorption unit; the temperature swing adsorption unit is provided with an adsorption bypass valve; and the air inlet end of the adsorption bypass valve is connected with the condensation recovery unit, and the air outlet end of the adsorption bypass valve is connected with the emptying unit. According to the invention, the resin adsorbent is selected and the desorption is carried out by using steam, so that vacuumizing is not required, equipment such as a vacuum pump, a cooling system and the like required by the traditional desorption mode is not required, the wall thickness of the adsorption tank is not required to be increased, the equipment is more simplified and ingenious, and the equipment cost is greatly reduced.
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
The emission limit of benzene which is an organic characteristic pollutant in waste gas of GB31571-2015 in the emission standard of pollutants in petrochemical industry is 4mg/m 3 Some places or enterprises will also have a benzene emission limit of 2mg/m at a stricter limit 3 To execute, the exhaust emission standard of VOCs is more and more strict, and then the traditional condensation and pressure swing adsorption (vacuum pump suction desorption) at the temperature of-70 DEG CThe system and the process face serious tests, and the benzene concentration in the tail gas emission exceeds the standard after 2-3 months although the benzene emission limit can be met in a short period; meanwhile, the active carbon has large proportion and also faces the cost pressure and environmental protection problems of solid waste generation during replacement.
Therefore, in order to achieve green emission, environment-friendly recycling and maximum recycling of benzene in tail gas, it is important to find a better condensation adsorption recycling system of benzene-containing gas.
Disclosure of Invention
The invention aims to: in order to overcome the defects in the prior art, the invention provides a condensing adsorption recovery system for benzene-containing gas.
The technical scheme is as follows: the invention provides a condensation adsorption recovery system for benzene-containing gas, which comprises a gas transmission unit, a condensation recovery unit connected with a gas transmission unit gas circuit, a compression condensation unit connected with a condensation recovery unit refrigeration pipeline, a temperature swing adsorption unit connected with the condensation recovery unit gas circuit, a condensate cooling recovery unit connected with a temperature swing adsorption unit liquid circuit, and an evacuation unit communicated with the temperature swing adsorption unit;
the temperature swing adsorption unit is provided with an adsorption bypass valve; the air inlet end of the adsorption bypass valve is connected with the condensation recovery unit, and the air outlet end of the adsorption bypass valve is connected with the evacuation unit;
the temperature swing adsorption unit comprises more than three adsorption tanks, and each adsorption tank is provided with 1 adsorption inlet valve, 1 adsorption outlet valve, 1 desorption inlet valve, 1 purge inlet valve and 1 desorption outlet valve which are matched with the adsorption tanks;
each desorption inlet valve is communicated with a desorption steam inlet; each purging inlet valve is communicated with a nitrogen inlet for purging;
the adsorption tanks of the temperature swing adsorption units all adopt spherical adsorption resin with the diameter of 0.3-1.2 mm as an adsorbent.
Preferably, the gas transmission unit comprises a gas transmission induced draft fan and a gas inlet flame arrester connected with a gas path of the gas transmission induced draft fan; the gas pipeline connected with the benzene-containing gas inlet at the gas inlet end of the gas inlet flame arrester is also provided with an oil gas pressure transmitter.
Preferably, the gas transmission induced draft fan is a variable frequency gas transmission induced draft fan, and the variable frequency gas transmission induced draft fan is controlled in an interlocking manner with the oil gas pressure transmitter.
Preferably, the upper part of each adsorption tank is provided with a steam flow equalizer.
Preferably, the condensation recovery unit comprises a multi-stage cold field heat exchanger and a first coalescer; the gas path inlet of the multistage cold field heat exchanger is communicated with the output end of the conveying induced draft fan; the gas path outlet of the multistage cold field heat exchanger is communicated with the pressure swing adsorption unit; the liquid outlet of the multistage cold field heat exchanger is communicated with the first coalescer; and the first coalescer is used for separating water in the condensate benzene and then outputting separated benzene and water respectively.
Preferably, the multistage cold field heat exchanger comprises a stage I cold field with the treatment temperature of 8+/-2 ℃, a stage II cold field with the treatment temperature of-30+/-5 ℃ and a stage III cold field with the treatment temperature of-70+/-5 ℃.
Preferably, the temperature swing adsorption unit comprises 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, a desorption inlet valve A, a desorption inlet valve B, a desorption inlet valve C, a desorption outlet valve A, a desorption outlet valve B, a desorption outlet valve C, an adsorption bypass valve, a purge inlet valve A, a purge inlet valve B and a purge inlet valve C;
the gas path outlet of the multistage cold-field heat exchanger is communicated with the inlet end of the adsorption bypass valve, the inlet end of the adsorption inlet valve A, the inlet end of the adsorption inlet valve B and the inlet end of the adsorption inlet valve C; the outlet end of the adsorption bypass valve is communicated with the emptying unit; the outlet end of the adsorption inlet valve A is communicated with the lower end of the adsorption tank A, the outlet end of the adsorption inlet valve B is communicated with the lower end of the adsorption tank B, and the outlet end of the adsorption inlet valve C is communicated with the lower end of the adsorption tank C.
Further preferably, in the temperature swing adsorption unit, temperature sensors are arranged at the upper section, the middle section and the lower section of the adsorption tank A, the adsorption tank B and the adsorption tank C, and the adsorption bypass valve, the gas transmission induced draft fan and the temperature sensors are controlled in an interlocking manner.
Still preferably, in the temperature swing adsorption unit, the tank body top ends of the adsorption tank a, the adsorption tank B and the adsorption tank C are all provided with safety valves, the tank body top ends of the adsorption tank a, the adsorption tank B and the adsorption tank C are also provided with pressure detectors, and the adsorption bypass valve, the gas transmission induced draft fan and the safety valves are controlled in an interlocking manner with each pressure detector.
Preferably, the upper end of the adsorption tank A is communicated with the inlet end of the adsorption outlet valve A, the upper end of the adsorption tank B is communicated with the inlet end of the adsorption outlet valve B, and the upper end of the adsorption tank C is communicated with the inlet end of the adsorption outlet valve C; the outlet end of the adsorption outlet valve A, the outlet end of the adsorption outlet valve B and the outlet end of the adsorption outlet valve C are communicated with the emptying unit.
Preferably, the inlet end of the desorption inlet valve a, the inlet end of the desorption inlet valve B and the inlet end of the desorption inlet valve C are all communicated with a steam inlet for desorption; the outlet end of the desorption inlet valve A is communicated with the upper end of the adsorption tank A, the outlet end of the desorption inlet valve B is communicated with the upper end of the adsorption tank B, and the outlet end of the desorption inlet valve C is communicated with the upper end of the adsorption tank C;
the inlet end of the purging inlet valve A, the inlet end of the purging inlet valve B and the inlet end of the purging inlet valve C are communicated with a nitrogen inlet for purging; the outlet end of the purging inlet valve A is communicated with the upper end of the adsorption tank A, the outlet end of the purging inlet valve B is communicated with the upper end of the adsorption tank B, and the outlet end of the purging inlet valve C is communicated with the upper end of the adsorption tank C;
the inlet end of the desorption outlet valve A is communicated with the lower end of the adsorption tank A, the inlet end of the desorption outlet valve B is communicated with the lower end of the adsorption tank B, and the inlet end of the desorption outlet valve C is communicated with the lower end of the adsorption tank C; the outlet end of the desorption outlet valve A, the outlet end of the desorption outlet valve B and the outlet end of the desorption outlet valve C are communicated with the condensate liquid recovery unit.
Preferably, the condensate cooling recovery unit comprises a multi-stage condenser and a second condenser;
the outlet end of the desorption outlet valve A, the outlet end of the desorption outlet valve B and the outlet end of the desorption outlet valve C are communicated with the air inlet end of the multistage condenser in the condensate liquid cooling recovery unit; the cold source of the multistage condenser is provided by circulating cooling water or circulating chilled water;
the air outlet end of the multistage condenser is connected with the air inlet end of the air inlet explosion-proof flame arrester; the liquid outlet end of the multistage condenser is communicated with the liquid inlet end of the second condenser; and the second coalescer is used for separating benzene in the condensed water and then outputting the separated benzene and water respectively.
Preferably, the emptying unit comprises an emptying cylinder, an air 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 emptying cylinder is communicated with an outlet end of the adsorption bypass valve, an outlet end of the adsorption outlet valve A, an outlet end of the adsorption outlet valve B and an outlet end of the adsorption outlet valve C through an outlet explosion-proof flame arrester.
Preferably, the compression condensing unit comprises a refrigeration compressor, a refrigeration condenser and a refrigeration unit expansion valve which are connected in sequence;
the other end of the expansion valve of the refrigeration unit is communicated with the refrigerant inlet of the multi-stage cold field heat exchanger, and the refrigerant outlet of the multi-stage cold field heat exchanger is communicated with the input end of the refrigeration compressor.
The beneficial effects are that: compared with the prior art, the condensing adsorption recovery system for the benzene-containing gas has the following advantages:
1. based on the structure and the structure provided by the invention, the adsorption tank of the temperature swing adsorption unit is filled with a specific resin adsorbent, the filling amount is small, the adsorbent does not need to be replaced, and only 5% of the adsorbent is needed to be supplemented each year; the operation cost is lower, and the mass production of solid waste is effectively reduced.
2. Compared with the traditional pressure swing adsorption (vacuum pump suction desorption), the condensing adsorption recovery system for benzene-containing gas provided by the invention selects a specific resin adsorbent and uses high-temperature steam for desorption/analysis, so that vacuumizing is not needed, on one hand, equipment such as a vacuum pump and a cooling system needed by a traditional desorption mode is not needed, on the other hand, the problem that the traditional activated carbon desorption needs vacuumizing, and the wall thickness of an adsorption tank needs to be increased to meet the safety requirement is effectively solved.
3. According to the condensing adsorption recovery system for benzene-containing gas, provided by the invention, the specific resin adsorbent is selected, high-temperature steam can be used for desorption under the structure and the structure of the condensing adsorption recovery system, nitrogen is used for purging and cooling, when the resin adsorbent is purged by nitrogen, the fine adsorbent can enter the sewage tank together with water and 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 purged after desorption is completed, black smoke is blown outwards by an evacuation cylinder when the activated carbon adsorbent is adsorbed, a vacuum pump and an adsorption valve are easy to be blocked by the carbon ash generated by the activated carbon adsorbent are effectively solved, the system is environment-friendly, the safety is higher, and the maintenance cost is effectively reduced.
Drawings
Fig. 1 is a schematic diagram of a condensation adsorption recovery system for benzene-containing gas according to one embodiment.
In the figure, 101-gas-conveying induced draft fan, 102-gas-inlet flame arrestor, 103-pressure transmitter, 201-multistage cold field heat exchanger, 202-first coalescer, 301-adsorption tank A, 302-adsorption tank B, 303-adsorption tank C, 304-adsorption inlet valve A, 305-adsorption inlet valve B, 306-adsorption inlet valve C, 307-adsorption outlet valve A, 308-adsorption outlet valve B, 309-adsorption outlet valve C, 310-desorption inlet valve A, 311-desorption inlet valve B, 312-desorption inlet valve C, 313-desorption outlet valve A, 314-desorption outlet valve B, 315-desorption outlet valve C, 316-adsorption bypass valve, 317-purge inlet valve A, 318-purge inlet valve B, 319-purge inlet valve C, 401-multistage condenser, 402-second condenser, 501-evacuation cylinder, 502-outlet flame arrestor, 503-concentration detector, 601-refrigeration compressor, 602-refrigeration condenser, 603-refrigeration unit expansion valve.
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 benzene-containing gas provided in this embodiment, as shown in fig. 1, includes a gas transmission unit 100, a condensation recovery unit 200 connected to a gas path of the gas transmission unit 100, a compression condensation unit 600 connected to a refrigeration pipeline of the condensation recovery unit 200, a temperature swing adsorption unit 300 connected to a gas path of the condensation recovery unit 200, a condensate cooling recovery unit 400 connected to a liquid path of the temperature swing adsorption unit 300, and an evacuation unit 500 connected to the temperature swing adsorption unit 300;
the temperature swing adsorption unit 300 is provided with an adsorption bypass valve 316; the adsorption bypass valve 316 has an inlet end connected to the condensation recovery unit 200 and an outlet end connected to the evacuation unit 500.
The gas transmission unit 100 comprises a gas transmission induced draft fan 101 and a gas inlet flame arrester 102 connected with a gas path of the gas transmission induced draft fan 101; the gas pipeline of which the gas inlet end is connected with the benzene-containing gas inlet is also provided with an oil gas pressure transmitter 103.
In this embodiment, the above-mentioned conveying induced draft fan (i.e. gas conveying induced draft fan) is a variable frequency type, which is controlled by the oil gas pressure transmitter installed on the conveying pipeline (i.e. gas conveying pipeline) in an interlocking manner, for example, when the pressure of the oil gas pressure transmitter reaches the starting value (adjustable between 200 and 400 Pa), the conveying induced draft fan is automatically started, and the benzene waste gas is introduced into the condensation adsorption recovery system; when the pressure of the oil gas pressure transmitter reaches a closing value (000-200 Pa is adjustable), the conveying induced draft fan is automatically closed, and no benzene waste gas is introduced into the condensing adsorption recovery system; for safety, the system is provided with an air inlet flame arrester at the front end of the air inlet and conveying induced draft fan, and the bidirectional flame arrester or detonation arrester can be selected according to the requirement of the distance of an air inlet pipeline.
Wherein the condensation recovery unit 200 comprises a multi-stage cold field heat exchanger 201 and a first coalescer 202; the gas path inlet of the multistage cold field heat exchanger 201 is communicated with the output end of the conveying induced draft fan 101; the gas path outlet of the multistage cold field heat exchanger 201 is communicated with the pressure swing adsorption unit 300; the liquid outlet of the multistage cold field heat exchanger 201 is communicated with the first coalescer 202; the first coalescer 202 separates water from the condensed benzene and outputs separated benzene and water, respectively, and the separated benzene and sewage are transported to a user-designated location. It can also be said that: benzene waste gas enters a first coalescer 202 to be subjected to benzene-water separation treatment through benzene condensate which is sequentially subjected to gradient cooling and condensation separation by a grade I cold field heat exchanger, a grade II cold field heat exchanger and a grade III cold field heat exchanger, and a small amount of separated sewage is subjected to appointed discharge.
In certain preferred embodiments, benzene-containing waste gas is introduced into a multistage cold field heat exchanger of a condensation recovery unit through a gas transmission induced draft fan, wherein the multistage cold field heat exchanger comprises a stage I cold field (benzene gas temperature is 8+/-2 ℃), a stage II cold field (benzene gas temperature is-30+/-5 ℃), and a stage III cold field (benzene gas temperature is-70+/-5 ℃), namely the multistage cold field heat exchanger comprises a stage I cold field with a treatment temperature of 8+/-2 ℃, a stage II cold field with a treatment temperature of-30+/-5 ℃) and a stage III cold field with a treatment temperature of-70+/-5 ℃); the cold source of the multistage cold field heat exchanger is provided by corresponding basic compression condensing units, and each basic compression condensing unit is sequentially provided with a refrigeration compressor, a refrigeration condenser, a refrigeration unit expansion valve and a cold field heat exchanger; the I-stage, II-stage and III-stage cold field of the refrigeration multi-stage cold field heat exchanger adopts two-module two-stage cascade Freon refrigeration: one module unit system carries out refrigeration, and when the pressure difference between the inlet and the outlet of the multi-stage cold field heat exchanger reaches a set value (such as 3-5 kPa lower than a gas transmission induced draft fan) or the refrigeration set time period, the system is switched to two module units for refrigeration; at the moment, one unit module enters a benzene melting defrosting mode, and enters a standby mode to wait for the next refrigerating mode after the benzene melting defrosting mode is finished, so that the continuous air inlet uninterrupted working mode of the system is ensured in a circulating and reciprocating mode. The temperature of benzene gas (namely benzene-containing gas) is sequentially cooled in a gradient manner in a three-stage cold field to be condensed and separated into condensate, and the condensate enters a first coalescer in a dead weight manner to be temporarily cached.
In some preferred embodiments, in the two-module two-stage cascade freon refrigeration adopted by the benzene gas condensate refrigeration equipment (namely, the multi-stage cold field heat exchanger 201), the multi-stage cold field heat exchanger 201 comprises two I-stage cold fields (benzene gas temperature is 8+/-2 ℃), two II-stage cold fields (benzene gas temperature is-30+/-5 ℃), and two III-stage cold fields (benzene gas temperature is-70+/-5 ℃); the freon in the I-stage cold field and the II-stage cold field heat exchangers is medium-temperature mixed refrigerant R404A (C2 HF5 pentafluoroethane: C2H2F4 tetrafluoroethane: C2H3F3 trifluoroethane=44%: 4%: 52%), and the freon in the III-stage cold field heat exchangers is low-temperature refrigerant R23 (CHF 3 trifluoromethane). Meanwhile, the multistage cold field heat exchanger 201 in the embodiment adopts a self-heating exhaust concurrent defrosting mode, so that the problem that benzene or water vapor is defrosted or frozen at a low temperature to block a gas path channel and cannot continuously run continuously in daily life is solved, and the benzene gas channel can be timely defrosted or frozen without being blocked. The method specifically comprises the following steps: a1 Freon channels in the I-level cold field heat exchanger, the II-level cold field heat exchanger and the III-level cold field heat exchanger adopt the direct heating of the hot exhaust gas of the compressor to defrost or melt ice; a2 A pipeline for hot exhaust defrosting or ice melting is automatically controlled by an explosion-proof electromagnetic valve to switch modes; a3 The hot exhaust of the compressors in the I-level, II-level and III-level cold field heat exchangers heats the oil outlet package of the I-level, II-level and III-level cold field heat exchange and simultaneously carries out fluorine cold recovery, thereby ensuring that the oil outlet pipeline is unblocked and not blocked; a4 The oil cooling recovery load can account for about 15% of the total condensation load (such as 14-16%, taking a set of 1000Nm3/h two-module two-stage cascade Freon refrigerating device as an example): the total refrigeration load is 145kW, and the oil cooling load is about 22 kW). Proved by experiments: the actually measured benzene gas concentration value of the benzene gas at the outlet of the multistage cold field heat exchanger provided by the embodiment can generally not exceed 1000mg/m < 3 >, so that the low-concentration benzene gas is subjected to a subsequent temperature swing adsorption unit, the operation load of the temperature swing adsorption unit can be effectively reduced, and a front-stage technical foundation is provided for the stable emission limit value of the benzene gas.
In some preferred embodiments, the first coalescer is a water-in-benzene separator, which can separate water from condensed liquid benzene well, and benzene with relatively high purity can be reused, so that the method is environment-friendly.
The temperature swing adsorption unit 300 includes an adsorption tank a301, an adsorption tank B302, an adsorption tank C303, an adsorption inlet valve a304, an adsorption inlet valve B305, an adsorption inlet valve C306, an adsorption outlet valve a307, an adsorption outlet valve B308, an adsorption outlet valve C309, a desorption inlet valve a310, a desorption inlet valve B311, a desorption inlet valve C312, a desorption outlet valve a313, a desorption outlet valve B314, a desorption outlet valve C315, an adsorption bypass valve 316, a purge inlet valve a317, a purge inlet valve B318, and a purge inlet valve C319;
the gas path outlet of the multistage cold-field heat exchanger 201 is communicated with the inlet end of the adsorption bypass valve 316, the inlet end of the adsorption inlet valve A304, the inlet end of the adsorption inlet valve B305 and the inlet end of the adsorption inlet valve C306; the outlet end of the adsorption bypass valve 316 communicates with the evacuation unit 500; the outlet end of the adsorption inlet valve A304 is communicated with the lower end of the adsorption tank A301, the outlet end of the adsorption inlet valve B305 is communicated with the lower end of the adsorption tank B302, and the outlet end of the adsorption inlet valve C306 is communicated with the lower end of the adsorption tank C303;
the upper end of the adsorption tank A301 is communicated with the inlet end of the adsorption outlet valve A307, the upper end of the adsorption tank B302 is communicated with the inlet end of the adsorption outlet valve B308, and the upper end of the adsorption tank C303 is communicated with the inlet end of the adsorption outlet valve C309; the outlet end of the adsorption-out valve A307, the outlet end of the adsorption-out valve B308 and the outlet end of the adsorption-out valve C309 are communicated with the evacuation unit 500;
the inlet end of the desorption inlet valve A310, the inlet end of the desorption inlet valve B311 and the inlet end of the desorption inlet valve C312 are communicated with a steam inlet for desorption; the outlet end of the desorption inlet valve A310 is communicated with the upper end of the adsorption tank A301, the outlet end of the desorption inlet valve B311 is communicated with the upper end of the adsorption tank B302, and the outlet end of the desorption inlet valve C312 is communicated with the upper end of the adsorption tank C303;
the inlet end of the purging inlet valve A317, the inlet end of the purging inlet valve B318 and the inlet end of the purging inlet valve C319 are communicated with a nitrogen inlet for purging; the outlet end of the purge inlet valve A317 is communicated with the upper end of the adsorption tank A301, the outlet end of the purge inlet valve B318 is communicated with the upper end of the adsorption tank B302, and the outlet end of the purge inlet valve C319 is communicated with the upper end of the adsorption tank C303;
the inlet end of the desorption outlet valve A313 is communicated with the lower end of the adsorption tank A301, the inlet end of the desorption outlet valve B311 is communicated with the lower end of the adsorption tank B302, and the inlet end of the desorption outlet valve C312 is communicated with the lower end of the adsorption tank C303; the outlet end of the desorption outlet valve a313, the outlet end of the desorption outlet valve B311 and the outlet end of the desorption outlet valve C312 are all communicated with the condensate liquid recovery unit 400.
The temperature swing adsorption unit mainly comprises three adsorption tanks and a plurality of adsorption/desorption valves. The three-tank adsorption can realize a third tank desorption mode of two adsorption tanks connected in parallel, which can be called as a (1+1)/1 mode (also can be called as a two-to-two parallel adsorption mode); one tank may be used to adsorb and desorb, and the third tank may be used in 1/1+1 mode (also referred to as one-off-one-standby mode or two-purpose one-standby mode).
The temperature swing adsorption unit adopts spherical adsorption resin with the diameter of 0.3-1.2 mm as an adsorbent, and the adsorption resin is a high molecular polymer, and has a porous three-dimensional structure, so that the adsorption unit is easy to regenerate, can be repeatedly used, and can reach extremely high separation and purification level. In this example, since the concentration of benzene-containing gas entering the adsorbent resin is low, the adsorption bed temperature is not excessively high (the temperature rise is not more than 5 ℃ C.).
In this embodiment, the temperature swing adsorption unit 300 has three adsorption tanks, 1 adsorption bypass valve, and a total of 16 or more control valves for each adsorption tank, including 1 adsorption inlet valve, 1 adsorption outlet valve, 1 desorption inlet valve, 1 purge inlet valve, and 1 desorption outlet valve. The temperature of an adsorption bed layer in the adsorption tank is detected at moment by temperature sensors (also can be temperature detectors) in the adsorption tank A, the adsorption tank B and the adsorption tank C in the temperature swing adsorption unit, and overtemperature prevention safety control is performed: when the temperature value of any temperature sensor exceeds a preset rapid-discharge temperature threshold value such as 55 ℃, the adsorption bypass valve 316 is opened to perform rapid discharge, and meanwhile, the gas transmission induced draft fan is closed to cut off the entry of benzene-containing gas, so that the safety measure can effectively prevent the temperature from exceeding the standard, and improve the operation safety; and the pressure detector is arranged at the top of each adsorption tank to detect the pressure of the adsorption bed layer in the adsorption tank at the moment, so that overpressure prevention safety control is performed: when the pressure value of any pressure detector exceeds a preset emergency discharge pressure threshold value, the adsorption bypass is carried out to directly discharge the air through the emptying cylinder and cut off the total air inlet (the air delivery induced draft fan is closed to cut off the benzene-containing gas), or the adsorption bypass is directly discharged through a safety valve (not shown in the figure) arranged at the top end of the tank body of the adsorption tank. In some preferred embodiments, corresponding measures are taken in time when the temperature exceeds or exceeds the pressure, such as adsorption bypass (adsorption bypass means that when the temperature swing adsorption unit only opens an adsorption bypass valve, gas flows through an evacuation cylinder to be discharged to the atmosphere through the adsorption bypass valve), and the total air intake is cut off through the evacuation cylinder to be discharged directly, or the total air intake is cut off through a safety valve arranged at the top end of a tank body of the adsorption tank (safety valve direct discharge means that when the pressure in the adsorption tank exceeds a set value of the safety valve, the safety valve is opened to discharge), so that the whole benzene gas treatment system is ensured to be safe and reliable. The safety valve is a valve arranged at the top end of each adsorption tank body, and is used for preventing overpressure.
The adsorption resin is a high molecular polymer, is characterized by adsorption, has a porous three-dimensional structure, is generally small spheres with the diameter of 0.3-1.2 mm, and has better adsorption performance as the particle size is smaller and more uniform. But the particle size is too small, the resistance to fluid is too large when in use, filtration is difficult, and the loss is easy. In certain preferred embodiments, the adsorbent filling in the adsorption tanks a, B, C of the temperature swing adsorption unit is: the spherical adsorption resin with a porous three-dimensional structure and the appearance of 0.3-1.2 mm in diameter generates little consumption, and only a certain amount of consumption is needed to be filled periodically, so that solid waste is hardly generated, and the problems of harm of solid waste generated by adsorption of activated carbon, cost for treating hazardous waste and the like are solved.
The internal structure of the adsorption resin is complex, like a pile of grape microspheres, the size of the grape microspheres is in the range of 0.06-0.5 mu m, and a plurality of gaps exist among the grape microspheres. It is this porous structure that gives resin excellent adsorption properties, is easy to regenerate, and can be used repeatedly, and can achieve extremely high levels of separation and purification.
In the above embodiment, two adsorption tanks in the three-tank adsorption are connected in parallel to attach a third tank desorption mode to illustrate the related working principle/working procedure: the gas (namely benzene-containing gas or benzene gas for short) output by the outlet of the condensation recovery unit is respectively fed into the adsorption tank A and the adsorption tank B through the adsorption inlet valve A and the adsorption inlet valve B, and after being subjected to strong adsorption of the adsorption resin under the conditions of about 10 ℃ and reasonable flow rate (generally between 0.05m/s and 0.25 m/s), the standard gas is discharged out of the temperature swing adsorption unit through the adsorption outlet valve A and the adsorption outlet valve B, and is discharged into the atmosphere through the outlet of the emptying cylinder after passing through the outlet flame arrestor. When the adsorption period reaches 1/2T (the general adsorption period T is 12-24 hours and is adjusted according to the actual benzene gas inlet concentration), the adsorption inlet valve A and the adsorption outlet valve A are closed, the adsorption inlet valve C and the adsorption outlet valve C are opened at the same time, and then the adsorption tank B and the adsorption tank C enter an adsorption mode; meanwhile, the adsorption tank A performs an analysis mode (namely, benzene waste gas condensed by the multistage cold-field heat exchanger 201 is connected in parallel through an adsorption inlet valve A304 and an adsorption inlet valve B305 and respectively enters an adsorption tank A301 and an adsorption tank B302, after being fully adsorbed by an adsorption resin bed layer, standard gas is discharged into the atmosphere through an evacuation unit 500 through an adsorption outlet valve A307 and an adsorption outlet valve B308, when adsorption meets a certain period, the adsorption inlet valve C306 and the adsorption outlet valve C309 are opened, the adsorption inlet valve A304 and the adsorption outlet valve A307 are closed at the same time, the adsorption tank A301 is switched to an analysis mode, and the adsorption tank B302 and the adsorption tank C303 are simultaneously adsorbed in two tanks, so that the total gas amount is large in contact with the adsorption resin bed layer, and the flow resistance is small): the desorption inlet valve A is opened, high-temperature steam (about 120 ℃) is evenly sprayed onto the adsorption resin from the top through the steam distributor (namely the steam flow equalizer), the high-temperature steam is in direct and full contact with the adsorption resin bed layer to carry out analysis regeneration of the adsorption resin, the analysis period is generally 1-2 hours and can be regenerated, at the moment, the desorption inlet valve A is closed, the purging inlet valve A is opened at the same time, nitrogen at normal temperature purges the adsorption resin bed layer, residual steam in the adsorption resin bed layer is purged, the adsorption resin bed layer is cooled, the purging work is completed when the temperature in the adsorption tank A is reduced to normal temperature, the purging period is generally completed within 1 hour, and the adsorption tank A enters a standby adsorption state at the moment. And the method is repeated in a circulating way (such as normal-temperature adsorption of a subsequent adsorption tank C and an adsorption tank A, high-temperature steam analysis and nitrogen purging cooling of the adsorption tank B are carried out for later use, and then normal-temperature adsorption of the adsorption tank A and the adsorption tank B is returned to, and the adsorption tank C is carried out for later use … … after high-temperature steam analysis and nitrogen purging cooling). And 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 desorption-nitrogen purging cooling modes, so that one adsorption period is completed.
When one adsorption tank is used alone to perform adsorption, one adsorption tank is used to perform analysis, and one adsorption tank is used in standby mode (for example, when adsorption tank A301 is used alone to perform adsorption, adsorption tank B30 is used to perform analysis, and adsorption tank C303 is used in standby mode), the operation of filling the adsorption resin into the third standby tank can be performed without stopping the adsorption system. In order to reduce the consumption of the adsorption resin, a 60-mesh filter screen is adopted at an air outlet port at the top (i.e. the upper end) of each adsorption tank, and a 60-mesh Y-shaped filter is arranged on a pipeline at the bottom (i.e. the lower end) of the adsorption tank. When each adsorption tank is analyzed, steam enters the upper part of the adsorption tank corresponding to the adsorption tank from the top steam inlet valve (namely the desorption inlet valve or the desorption inlet valve) (for example, the steam enters the upper part of the adsorption tank A301 from the top desorption inlet valve A310), and each adsorption tank upper part is provided with a steam flow equalizer (namely a steam distributor) device so that the steam is uniformly sprayed, the steam outlet surface covers the whole upper adsorbent bed, the steam consumption is saved, and the generation of steam condensate is reduced.
Wherein the condensate cooling recovery unit 400 includes a multi-stage condenser 401 and a second condenser 402;
the outlet end of the desorption outlet valve A313, the outlet end of the desorption outlet valve B311 and the outlet end of the desorption outlet valve C312 are communicated with the air inlet end of the multistage condenser 401 in the condensate liquid recovery unit 400; the cold source of the multistage condenser 401 is provided by circulating cooling water or circulating chilled water;
the air outlet end of the multistage condenser 401 is connected with the air inlet end of the air inlet explosion-proof flame arrester 102; the liquid outlet end of the multistage condenser 401 is communicated with the liquid inlet end of the second condenser 402; the second coalescer 402 separates benzene from the condensed water, and outputs the separated benzene and water, respectively, and delivers the separated benzene and water to a user-designated location. In this embodiment, the steam after analysis is cooled to condensed water at 15-20 ℃ in the multistage condenser 401, and contains a small amount of benzene in the analysis liquid, and the condensed water enters the second condenser 402 to be subjected to water-benzene separation treatment, and the separated small amount of benzene liquid can be recycled.
The condensed water obtained by the steam analysis enters a multistage condenser after passing through a desorption outlet valve A, a desorption outlet valve B and a desorption outlet valve C or saturated gas blown by nitrogen passes through the desorption outlet valve A, the desorption outlet valve B and the desorption outlet valve C. Condensed water or saturated gas is cooled in sequence by multiple stages of refrigerants (such as circulating cooling water or circulating chilled water or other refrigerants), and then the condensed water at normal temperature enters a second condenser.
In some preferred embodiments, the second coalescer is a benzene-in-water separator which can well separate benzene from condensate water, and condensate water with relatively low content can be directly discharged, so that cost input caused by secondary treatment of sewage is reduced.
Wherein the evacuation unit 500 includes an evacuation cartridge 501, an outlet flame arrestor 502, and 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 air inlet of the emptying cartridge 501 communicates with the outlet end of the adsorption bypass valve 316, the outlet end of the adsorption outlet valve a307, the outlet end of the adsorption outlet valve B308, and the outlet end of the adsorption outlet valve C309 through an outlet explosion-proof flame arrester 502.
The compression condensing unit 600 includes a refrigeration compressor 601, a refrigeration condenser 602, and a refrigeration unit expansion valve 603, which are sequentially connected;
the other end of the expansion valve 603 of the refrigeration unit is communicated with the refrigerant inlet of the multi-stage cold-field heat exchanger 201, and the refrigerant outlet of the multi-stage cold-field heat exchanger 201 is communicated with the input end of the refrigeration compressor 601.
As shown in fig. 1, in the condensation adsorption recovery system provided in this embodiment, benzene waste gas conveyed by the gas conveying unit 100 is sent to the condensation recovery unit 200 through the variable frequency gas conveying induced draft fan 101, and condensate liquid output after multi-stage condensation cooling is discharged/collected after water separation treatment in benzene is performed through the first coalescer; the low-concentration waste gas which is output after being condensed and cooled by the multi-stage cold field heat exchanger 201 enters the temperature swing adsorption unit 300, and after being adsorbed by the special adsorption resin, the tail gas reaching the standard is discharged by the evacuation unit 500;
the temperature swing adsorption unit 300 operates in the following modes: alternately performing normal-temperature adsorption, steam analysis and nitrogen purging according to a set period; the gas after the gas-liquid mixture obtained by steam analysis and nitrogen sweeping is cooled by the multi-stage condenser 401 returns to the front end of the gas-conveying induced draft fan 101 to perform condensation adsorption discharge treatment process again; the liquid of the gas-liquid mixture cooled by the multi-stage condenser 401 after the steam analysis and nitrogen sweeping is discharged/collected after being treated by benzene separation in water by the second coalescer.
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 benzene offgas or benzene gas described herein may also be referred to as benzene-containing offgas or benzene-containing gas, and may also be referred to as benzene gas for short. The desorption inlet valve described herein may also be referred to as a desorption inlet valve or a vapor inlet valve. The desorption valve described herein may also be referred to as a desorption valve or a vapor outlet valve. As used herein, a (where "adsorption inlet valve, adsorption outlet valve, desorption inlet valve, purge inlet valve, desorption outlet valve, etc.) 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 "/" herein indicates or.
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 (10)
1. A condensation adsorption recovery system for benzene-containing gas, its characterized in that: the device comprises a gas transmission unit (100), a condensation recovery unit (200) connected with a gas path of the gas transmission unit (100), a compression condensation unit (600) connected with a refrigeration pipeline of the condensation recovery unit (200), a temperature swing adsorption unit (300) connected with the gas path of the condensation recovery unit (200), a condensate cooling recovery unit (400) connected with a liquid path of the temperature swing adsorption unit (300), and an evacuation unit (500) communicated with the temperature swing adsorption unit (300);
the temperature swing adsorption unit (300) is provided with an adsorption bypass valve (316); the air inlet end of the adsorption bypass valve (316) is connected with the condensation recovery unit (200), and the air outlet end is connected with the emptying unit (500);
the temperature swing adsorption unit (300) comprises more than three adsorption tanks, and each adsorption tank is provided with 1 adsorption inlet valve, 1 adsorption outlet valve, 1 desorption inlet valve, 1 purge inlet valve and 1 desorption outlet valve which are matched with the adsorption tanks;
each desorption inlet valve is communicated with a desorption steam inlet; each purging inlet valve is communicated with a nitrogen inlet for purging;
the adsorption tanks of the temperature swing adsorption units all adopt spherical adsorption resin with the diameter of 0.3-1.2 mm as an adsorbent.
2. The condensation adsorption recovery system for benzene-containing gas according to claim 1, wherein: the gas transmission unit (100) comprises a gas transmission induced draft fan (101) and a 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 the gas pipeline of which the gas inlet end of the gas inlet flame arrester (102) is connected with the benzene-containing gas inlet;
the gas transmission induced draft fan (101) is a variable-frequency gas transmission induced draft fan and is controlled in an interlocking manner with the oil gas pressure transmitter (103); and/or
The upper part of each adsorption tank is provided with a steam flow equalizer.
3. The condensation adsorption recovery system for benzene-containing gas according to claim 2, wherein: the condensation recovery unit (200) comprises a multi-stage cold field heat exchanger (201) and a first coalescer (202); the gas path inlet of the multistage cold field heat exchanger (201) is communicated with the output end of the conveying induced draft fan (101); the gas path outlet of the multistage cold field heat exchanger (201) is communicated with the pressure swing adsorption unit (300); the liquid outlet of the multistage cold field heat exchanger (201) is communicated with the first coalescer (202); the first coalescer (202) is used for separating water in the condensate benzene and then outputting separated benzene and water respectively;
the multistage cold field heat exchanger comprises a stage I cold field with the treatment temperature of 8+/-2 ℃, a stage II cold field with the treatment temperature of-30+/-5 ℃ and a stage III cold field with the treatment temperature of-70+/-5 ℃.
4. The condensation adsorption recovery system for benzene-containing gas according to claim 3, wherein: the temperature swing adsorption unit (300) comprises an adsorption tank A (301), an adsorption tank B (302), an adsorption tank C (303), an adsorption inlet valve A (304), an adsorption inlet valve B (305), an adsorption inlet valve C (306), an adsorption outlet valve A (307), an adsorption outlet valve B (308), an adsorption outlet valve C (309), a desorption inlet valve A (310), a desorption inlet valve B (311), a desorption inlet valve C (312), a desorption outlet valve A (313), a desorption outlet valve B (314), a desorption outlet valve C (315), an adsorption bypass valve (316), a purge inlet valve A (317), a purge inlet valve B (318) and a purge inlet valve C (319);
the gas path outlet of the multistage cold-field heat exchanger (201) is communicated with the inlet end of an adsorption bypass valve (316), the inlet end of an adsorption inlet valve A (304), the inlet end of an adsorption inlet valve B (305) and the inlet end of an adsorption inlet valve C (306); an outlet end of the adsorption bypass valve (316) is communicated with the evacuation unit (500); the outlet end of the adsorption inlet valve A (304) is communicated with the lower end of the adsorption tank A (301), the outlet end of the adsorption inlet valve B (305) is communicated with the lower end of the adsorption tank B (302), and the outlet end of the adsorption inlet valve C (306) is communicated with the lower end of the adsorption tank C (303).
5. The condensation adsorption recovery system for benzene-containing gas as claimed in claim 4, wherein:
in the temperature swing adsorption unit, temperature sensors are arranged at the upper section, the middle section and the lower section of an adsorption tank A (301), an adsorption tank B (302) and an adsorption tank C (303), and an adsorption bypass valve (316), a gas transmission induced draft fan (101) and the temperature sensors are controlled in an interlocking mode.
6. The condensation adsorption recovery system for benzene-containing gas as claimed in claim 4, wherein:
in the temperature swing adsorption unit, the tank body top ends of the adsorption tank A (301), the adsorption tank B (302) and the adsorption tank C (303) are respectively provided with a safety valve, the tank body top ends of the adsorption tank A (301), the adsorption tank B (302) and the adsorption tank C (303) are also provided with pressure detectors, and the adsorption bypass valve (316), the gas transmission induced draft fan (101) and the safety valves are respectively controlled in an interlocking manner with the pressure detectors.
7. The condensation adsorption recovery system for benzene-containing gas as claimed in claim 4, wherein: the upper end of the adsorption tank A (301) is communicated with the inlet end of the adsorption outlet valve A (307), the upper end of the adsorption tank B (302) is communicated with the inlet end of the adsorption outlet valve B (308), and the upper end of the adsorption tank C (303) is communicated with the inlet end of the adsorption outlet valve C (309); the outlet end of the adsorption-out valve A (307), the outlet end of the adsorption-out valve B (308) and the outlet end of the adsorption-out valve C (309) are communicated with the emptying unit (500).
8. The condensation adsorption recovery system for benzene-containing gas as claimed in claim 4, wherein: the inlet end of the desorption inlet valve A (310), the inlet end of the desorption inlet valve B (311) and the inlet end of the desorption inlet valve C (312) are communicated with a desorption steam inlet; the outlet end of the desorption inlet valve A (310) is communicated with the upper end of the adsorption tank A (301), the outlet end of the desorption inlet valve B (311) is communicated with the upper end of the adsorption tank B (302), and the outlet end of the desorption inlet valve C (312) is communicated with the upper end of the adsorption tank C (303);
the inlet end of the purging inlet valve A (317), the inlet end of the purging inlet valve B (318) and the inlet end of the purging inlet valve C (319) are communicated with a nitrogen inlet for purging; the outlet end of the purging inlet valve A (317) is communicated with the upper end of the adsorption tank A (301), the outlet end of the purging inlet valve B (318) is communicated with the upper end of the adsorption tank B (302), and the outlet end of the purging inlet valve C (319) is communicated with the upper end of the adsorption tank C (303);
the inlet end of the desorption outlet valve A (313) is communicated with the lower end of the adsorption tank A (301), the inlet end of the desorption outlet valve B (311) is communicated with the lower end of the adsorption tank B (302), and the inlet end of the desorption outlet valve C (312) is communicated with the lower end of the adsorption tank C (303); the outlet end of the desorption outlet valve A (313), the outlet end of the desorption outlet valve B (311) and the outlet end of the desorption outlet valve C (312) are communicated with the condensate cooling recovery unit (400).
9. The condensation adsorption recovery system for benzene-containing gas as claimed in claim 4, wherein: the condensate cooling recovery unit (400) comprises a multistage condenser (401) and a second condenser (402);
the outlet end of the desorption outlet valve A (313), the outlet end of the desorption outlet valve B (311) and the outlet end of the desorption outlet valve C (312) are communicated with the air inlet end of a multistage condenser (401) in the condensate cooling recovery unit (400); the cold source of the multistage condenser (401) is provided by circulating cooling water or circulating chilled water;
the air outlet end of the multistage condenser (401) is connected with the air inlet end of the air inlet explosion-proof flame arrester (102); the liquid outlet end of the multistage condenser (401) is communicated with the liquid inlet end of the second condenser (402); the second coalescer (402) separates benzene in the condensed water and outputs separated benzene and water respectively.
10. The condensation adsorption recovery system for benzene-containing gas as claimed in claim 4, wherein: the evacuation unit (500) comprises an evacuation cylinder (501), an air 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 emptying cylinder (501) is communicated with an outlet end of the adsorption bypass valve (316), an outlet end of the adsorption outlet valve A (307), an outlet end of the adsorption outlet valve B (308) and an outlet end of the adsorption outlet valve C (309) through an outlet explosion-proof flame arrester (502);
the compression condensing unit (600) comprises a refrigeration compressor (601), a refrigeration condenser (602) and a refrigeration unit expansion valve (603) which are connected in sequence;
the other end of the expansion valve (603) of the refrigeration unit is communicated with a refrigerant inlet of the multistage cold-field heat exchanger (201), and a refrigerant outlet of the multistage cold-field heat exchanger (201) is communicated with an input end of the refrigeration compressor (601).
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| CN202311687603.9A CN117619087A (en) | 2023-12-09 | 2023-12-09 | Condensing adsorption recovery system for benzene-containing gas |
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| CN202311687603.9A CN117619087A (en) | 2023-12-09 | 2023-12-09 | Condensing adsorption recovery system for benzene-containing gas |
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