CN210511720U - Direct-fired backflow high-efficiency organic waste gas treatment system - Google Patents
Direct-fired backflow high-efficiency organic waste gas treatment system Download PDFInfo
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- CN210511720U CN210511720U CN201920253816.3U CN201920253816U CN210511720U CN 210511720 U CN210511720 U CN 210511720U CN 201920253816 U CN201920253816 U CN 201920253816U CN 210511720 U CN210511720 U CN 210511720U
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- 239000007789 gas Substances 0.000 title claims abstract description 296
- 239000010815 organic waste Substances 0.000 title claims abstract description 24
- 239000000428 dust Substances 0.000 claims abstract description 105
- 238000001179 sorption measurement Methods 0.000 claims abstract description 84
- 238000011084 recovery Methods 0.000 claims abstract description 74
- 239000002912 waste gas Substances 0.000 claims abstract description 26
- 238000010992 reflux Methods 0.000 claims abstract 3
- 238000003795 desorption Methods 0.000 claims description 85
- 238000001816 cooling Methods 0.000 claims description 44
- 239000000112 cooling gas Substances 0.000 claims description 41
- 238000004891 communication Methods 0.000 claims description 30
- 238000007664 blowing Methods 0.000 claims description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 4
- 239000002131 composite material Substances 0.000 claims description 3
- 239000003500 flue dust Substances 0.000 claims description 2
- 239000003595 mist Substances 0.000 claims description 2
- 230000003134 recirculating effect Effects 0.000 claims 2
- 238000002485 combustion reaction Methods 0.000 abstract description 9
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 abstract description 8
- 239000000377 silicon dioxide Substances 0.000 abstract description 5
- 125000004122 cyclic group Chemical group 0.000 abstract description 4
- 238000000926 separation method Methods 0.000 abstract description 3
- 235000012239 silicon dioxide Nutrition 0.000 abstract description 2
- 238000013461 design Methods 0.000 description 8
- 238000010586 diagram Methods 0.000 description 7
- 238000007599 discharging Methods 0.000 description 6
- 238000004064 recycling Methods 0.000 description 6
- 239000002245 particle Substances 0.000 description 5
- 239000004065 semiconductor Substances 0.000 description 3
- 238000012546 transfer Methods 0.000 description 3
- 229910021536 Zeolite Inorganic materials 0.000 description 2
- 238000003915 air pollution Methods 0.000 description 2
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 239000010457 zeolite Substances 0.000 description 2
- 229910004298 SiO 2 Inorganic materials 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000000034 method Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
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Abstract
A direct-combustion reflux high-efficiency organic waste gas treatment system is characterized in that the exhaust gas of a direct-combustion incinerator can be subjected to heat recovery through at least more than three heat exchangers, and the exhaust gas of the direct-combustion incinerator is subjected to heat exchange through one heat exchanger and the exhaust gas (adsorption treatment gas) of a clean gas discharge pipeline at an outlet of an adsorption area, so that the exhaust gas is cooled and then conveyed into dust removal equipment to carry out dust or silicon dioxide (SiO)2) And after the separation of oxides, finally, conveying the gas output by the dust removal equipment to the waste gas inlet pipeline, so that the combusted gas can enter an adsorption area of the adsorption rotating wheel for cyclic utilization and is not discharged through the chimney, the discharge amount of the chimney can be reduced, and the treatment efficiency of the organic waste gas can be improved.
Description
Technical Field
The utility model relates to a direct combustion backward flow high efficiency organic waste gas treatment system especially relates to one kind and is used for getting into the gas after the burning and should adsorb the adsorption zone cyclic utilization of runner, and does not discharge through this chimney, makes organic waste gas's treatment effeciency can promote, and is applicable to the organic waste gas treatment system or the similar equipment of semiconductor industry, photoelectric industry or the relevant industry of chemistry.
Background
At present, volatile organic gases (VOC) are generated in the manufacturing and production processes of the semiconductor industry or the photoelectric industry, and therefore, processing equipment for processing the VOC is installed in each factory to prevent the VOC from being directly discharged into the air to cause air pollution. At present, most of the concentrated gas desorbed by the treatment equipment is delivered to the incinerator for combustion, and the combusted gas is delivered to a chimney for emission.
However, in recent years, air pollution has been very important to the central government or local governments, and therefore, the emission standards of the stack have been made about the suspended Particles (PM)10) And fine suspended Particles (PM)2.5) According to the air quality standard of (1), and based on the results of the domestic health impact research, the health impact is considered as the priority, the' fine suspended Particles (PM)2.5) The 24 hour value is defined as 35 mu g/m3The annual average value is defined as 15 mu g/m3. And Taiwan environmental protection agency of China primarily defines Taiwan 109(2020) to achieve annual average value of fine suspended particle concentration of 15 μ g/m in Taiwan3Will develop according to the international regulatory trendExamining its fine suspended Particles (PM)2.5) Air quality standard and the standard value of air quality (24 hours value is defined as 25 μ g/m) proposed by WHO3The annual average value is defined as 10 mu g/m3) The air quality improvement target is achieved.
Therefore, in view of the above-mentioned shortcomings, the inventors of the present invention have expected to provide a direct-fired, high-efficiency organic waste gas treatment system with improved organic waste gas treatment efficiency, which is easy to operate and assemble by the user, and thus have earnestly studied, designed, assembled and manufactured to provide convenience to the user.
SUMMERY OF THE UTILITY MODEL
The main objective of the present invention is to provide a direct-fired backflow high-efficiency organic waste gas treatment system, which mainly recovers heat of the exhaust gas of a direct-fired incinerator via at least three heat exchangers, exchanges heat of the exhaust gas of the direct-fired incinerator via a heat exchanger and the exhaust gas (adsorption treatment gas) of the clean gas discharge pipeline of the outlet of the adsorption area, cools the exhaust gas, and conveys the exhaust gas to the dust removal equipment to perform dust or silicon dioxide (SiO)2) After the separation of oxide, will be carried this waste gas admission line by the gas that this dust collecting equipment exported again at last, make the gas after the burning can get into the adsorption zone cyclic utilization of this absorption runner, and not discharge through this chimney, let the emission capacity of this chimney reduce to make the treatment effeciency of organic waste gas can promote, and then increase holistic practicality.
Another objective of the present invention is to provide a direct-fired backflow high-efficiency organic waste gas treatment system, through being equipped with an intercommunication pipeline between this cooling gas conveying pipeline and this hot gas conveying pipeline, and this intercommunication pipeline is equipped with an intercommunication control valve, and this hot gas conveying pipeline is equipped with a hot gas control valve, and form the proportion air door through this intercommunication control valve and this hot gas control valve, therefore, the efficiency that has the proportion air door is formed through the design of this intercommunication control valve and this hot gas control valve, so as to be able to adjust and control the size of wind-force, let the temperature in this hot gas conveying pipeline can keep certain high temperature to offer the desorption district that should adsorb the runner and use, and have the efficiency of the energy can be saved, and then increase holistic usability.
Another objective of the present invention is to provide a direct-fired backflow high-efficiency organic waste gas treatment system and method thereof, a communicating pipeline is disposed between the cooling gas conveying pipeline and the hot gas conveying pipeline, and the communicating pipeline is provided with a communicating control valve, and the cooling gas conveying pipeline is provided with a cooling air control valve, and a proportional air door is formed through the communicating control valve and the cooling air control valve, thereby forming an efficiency with the proportional air door through the design of the communicating control valve and the cooling air control valve, so as to adjust and control the size of wind power, so that the temperature in the hot gas conveying pipeline can keep a certain high temperature to be provided for the desorption area of the adsorption rotating wheel, and the efficiency of energy saving is provided, and the whole operability is increased.
In order to further understand the features, characteristics and technical contents of the present invention, please refer to the following detailed description and the accompanying drawings, which are provided for reference and illustration only, and are not used to limit the present invention.
Drawings
Fig. 1 is a schematic diagram of a main structure of a first embodiment of the present invention;
fig. 2 is a schematic structural diagram of a first proportional damper according to a first embodiment of the present invention;
fig. 3 is a schematic structural diagram of a second proportional damper according to a first embodiment of the present invention;
FIG. 4 is a schematic diagram of a second embodiment of the present invention;
fig. 5 is a schematic structural diagram of a first proportional damper according to a second embodiment of the present invention;
fig. 6 is a schematic structural diagram of a second proportional damper according to a second embodiment of the present invention.
10. Direct combustion type incinerator 11, air inlet
12. Air outlet 20 and adsorption runner
201. Adsorption zone 202, cooling zone
203. Desorption zone 21, waste gas inlet line
22. Clean gas discharge pipeline 221 and windmill
23. Cooling gas inlet line 231, gas bypass line
24. Cooling gas delivery pipe 241, cooling gas control valve
25. Hot gas conveying pipeline 251 and hot gas control valve
26. Desorption concentrated waste gas pipeline 27 and communication pipeline
271. Communication control valve 30, first heat exchanger
301. A first cold side duct 302, a first hot side duct
31. A first hot gas recovery pipeline 32, a first incineration hot gas recovery pipeline
33. First desorption concentrated gas conveying pipeline 40 and second heat exchanger
401. A second cold side duct 402, a second hot side duct
50. Third heat exchanger 501, third cold side piping
502. Third hot side pipeline
51. Third desorption concentrated gas conveying pipeline
52. Third hot gas recovery line 60, fourth heat exchanger
601. A fourth cold side duct 602 and a fourth hot side duct
61. A fourth desorption concentrated gas delivery pipeline 62 and a fourth hot gas recovery pipeline
70. Fifth heat exchanger 701, fifth cold side piping
702. Fifth hot side pipeline 71 and fifth hot gas recovery pipeline
80. Dust removing equipment 81 and dust removing air inlet pipeline
82. Dust removal air outlet pipeline 821 and windmill
90. Chimney 91, chimney exhaust line
Detailed Description
Please refer to fig. 1 to 6, which are schematic diagrams illustrating an embodiment of the present invention. The best mode of the direct-fired backflow high-efficiency organic waste gas treatment system is applied to a volatile organic waste gas treatment system or similar equipment in the semiconductor industry, the photoelectric industry or the chemical related industry, and mainly enables combusted gas to enter the adsorption area of the adsorption rotating wheel for cyclic utilization, and the combusted gas is not discharged through the chimney, so that the treatment efficiency of organic waste gas can be improved.
The first embodiment of the present invention is a direct-fired backflow high-efficiency organic waste gas treatment system, which is mainly provided with a direct-fired incinerator 10, an adsorption rotating wheel 20, a first heat exchanger 30, a second heat exchanger 40, a third heat exchanger 50, a fifth heat exchanger 70, a dust-removing device 80, and a chimney 90 (as shown in fig. 1 to 3), wherein the first heat exchanger 30 is provided with a first cold-side pipeline 301 and a first hot-side pipeline 302, the second heat exchanger 40 is provided with a second cold-side pipeline 401 and a second hot-side pipeline 402, the third heat exchanger 50 is provided with a third cold-side pipeline 501 and a third hot-side pipeline 502, the fifth heat exchanger 70 is provided with a fifth cold-side pipeline 701 and a fifth hot-side pipeline 702, and the dust-removing device 80 is provided with a bag-type dust remover, an electric bag-type composite dust remover, an inertial dust remover, an electrostatic dust remover, a centrifugal dust remover, and a chimney 90 (as, The direct-fired incinerator (TO)10 is provided with an air inlet 11 and an air outlet 12, and the direct-fired incinerator (TO)10 is internally provided with a furnace end and a hearth, so that the organic waste gas can enter the furnace end from the air inlet 11 TO be combusted, and the combusted gas can pass through the hearth and be discharged from the air outlet 12.
The adsorption rotor 20 is a zeolite concentration rotor or a concentration rotor made of other materials, and the adsorption rotor 20 is provided with an adsorption region 201, a cooling region 202 and a desorption region 203, the adsorption rotor 20 is provided with a waste gas inlet pipeline 21, a clean gas discharge pipeline 22, a cooling gas inlet pipeline 23, a cooling gas delivery pipeline 24, a hot gas delivery pipeline 25 and a desorption concentration waste gas pipeline 26 (as shown in fig. 1 to 3), and the other end of the waste gas inlet pipeline 21 is connected to one side of the adsorption region 201 of the adsorption rotor 20, so that the adsorption region 201 of the adsorption rotor 20 can adsorb the waste gas in the waste gas inlet pipeline 21, and one end of the clean gas discharge pipeline 22 is connected to the other side of the adsorption region 201 of the adsorption rotor 20, so that the waste gas is purified by the adsorption region 201 of the adsorption rotor 20 and then is delivered by the clean gas discharge pipeline 22.
In addition, one end of the cooling air inlet pipe 23 is connected to one side of the cooling area 202 of the sorption rotor 20, and the cooling air inlet pipe 23 has two embodiments, wherein the first embodiment is that the cooling air inlet pipe 23 is used for entering external air (as shown in fig. 1 and fig. 2), and the external air is fresh air, so as to convey the external air into the cooling area 202 of the sorption rotor 20 for cooling, and the second embodiment is that a gas bypass pipe 231 (as shown in fig. 3) is provided on the cooling air inlet pipe 23, one end of the gas bypass pipe 231 is connected to the cooling air inlet pipe 23, and the other end of the gas bypass pipe 231 is connected to the exhaust gas inlet pipe 21, so as to convey part of the exhaust gas into the cooling area 203 of the sorption rotor 20 for cooling through the gas bypass pipe 231.
In addition, one end of the cooling gas conveying pipeline 24 is connected to the other side of the cooling region 203 of the adsorption rotor 20, the other end of the cooling gas conveying pipeline 24 is connected to one end of the second cold-side pipeline 401 of the second heat exchanger 40, so as to convey the cooling gas in the cooling gas conveying pipeline 24 into the second heat exchanger 40 for heat exchange (as shown in fig. 1 to 3), the other end of the second cold-side pipeline 401 of the second heat exchanger 40 is connected to the other end of the hot gas conveying pipeline 25, one end of the hot gas conveying pipeline 25 is connected to the other side of the desorption region 203 of the adsorption rotor 20, one side of the desorption region 203 of the adsorption rotor 20 is connected to one end of the desorption concentrated gas pipeline 26, so that the hot gas lifted by the second heat exchanger 50 can be conveyed to the desorption region 203 of the adsorption rotor 20 for desorption through the hot gas conveying pipeline 25, and the desorption concentrated gas desorbed at high temperature can be transported through the desorption concentrated gas pipeline 26.
In addition, a proportional damper is provided between the cooling gas delivery pipeline 24 and the hot gas delivery pipeline 25 in the first embodiment of the present invention, and the proportional damper has two implementation designs, wherein the first implementation design is to provide a communication pipeline 27 between the cooling gas delivery pipeline 24 and the hot gas delivery pipeline 25, and the communication pipeline 27 is provided with a communication control valve 271, and the hot gas delivery pipeline 25 is provided with a hot gas control valve 251 (as shown in fig. 2), and the proportional damper is formed by the communication control valve 271 and the hot gas control valve 25, and the second implementation design is to provide a communication pipeline 27 between the cooling gas delivery pipeline 24 and the hot gas delivery pipeline 25, and the communication pipeline 27 is provided with a communication control valve 271, and the cooling gas delivery pipeline 24 is provided with a cooling control valve 241 (as shown in fig. 3), and a proportional damper is formed by the communication control valve 271 and the cooling control valve 241, so that the magnitude of the wind force can be adjusted and controlled regardless of the proportional damper designed by the communication control valve 271 and the hot gas control valve 251 or the proportional damper designed by the communication control valve 271 and the cooling control valve 241, and the temperature in the hot gas delivery pipeline 25 can be kept at a certain high temperature to be provided for the desorption region 203 of the adsorption rotor 20.
Furthermore, the third heat exchanger 50 is connected to a third desorption concentrated gas transportation pipeline 51 and a third hot gas recovery pipeline 52, one end of the third cold-side pipeline 51 of the third heat exchanger 50 is connected to the other end of the desorption concentrated gas pipeline 26 (as shown in fig. 1 to 3), one end of the third desorption concentrated gas transportation pipeline 51 is connected to the other end of the third cold-side pipeline 501 of the third heat exchanger 50, the other end of the third desorption concentrated gas transportation pipeline 51 is connected to one end of the first cold-side pipeline 301 of the first heat exchanger 30, one end of the third hot gas recovery pipeline 52 is connected to one end of the third hot-side pipeline 502 of the third heat exchanger 50, and the other end of the third hot gas recovery pipeline 52 is connected to the other end of the second hot-side pipeline 402 of the second heat exchanger 40. Thus, the concentrated desorption gas desorbed from the desorption region 203 of the adsorption rotor 20 can be transferred to the third cold-side pipe 502 of the third heat exchanger 50 through the concentrated desorption gas pipe 26 for heat exchange, and further transferred to the first cold-side pipe 301 of the first heat exchanger 30 through the third concentrated desorption gas pipe 51 for heat exchange.
In addition, the first heat exchanger 30 is connected to a first hot gas recycling pipeline 31, a first incinerating hot gas recycling pipeline 32 and a first desorption concentrated gas delivery pipeline 33, wherein one end of the first incineration hot gas recovery pipe 32 is connected to one end of the first hot side pipe 302 of the first heat exchanger 30, the other end of the first incineration hot gas recovery line 32 is connected to the gas outlet 12 of the direct combustion incinerator 10 (as shown in figures 1 to 3), one end of the first hot gas recovery pipe 31 is connected to the other end of the first hot side pipe 302 of the first heat exchanger 30, the other end of the first hot gas recovery pipe 31 is connected to one end of the second hot side pipe 402 of the second heat exchanger 40, one end of the first desorption concentrated gas transfer line 33 is connected to the other end of the first cold-side line 301 of the first heat exchanger 30, the other end of the first desorption concentrated gas delivery pipeline 33 is connected with the gas inlet 11 of the direct-fired incinerator 10. Therefore, the concentrated desorption gas delivered through the first cold-side pipeline 301 of the first heat exchanger 30 can be delivered to the gas inlet 11 of the direct-fired incinerator 10 through the first concentrated desorption gas delivery pipeline 33, the gas combusted by the direct-fired incinerator 10 can be delivered into the first hot-side pipeline 302 of the first heat exchanger 30 through the first hot gas recovery pipeline 32 through the gas outlet 12 for heat recovery, and the gas is delivered into the second hot-side pipeline 402 of the second heat exchanger 40 through the first hot gas recovery pipeline 31 for heat recovery, and then the gas is delivered into the third hot-side pipeline 502 of the third heat exchanger 50 through the third hot gas recovery pipeline 52 for heat recovery.
A fifth hot gas recovery pipeline 71 is connected to the fifth heat exchanger 70, one end of a fifth cold side pipeline 701 of the fifth heat exchanger 70 is connected to the other end of the clean gas discharge pipeline 22, one end of the fifth hot gas recovery pipeline 71 is connected to one end of a fifth hot side pipeline 702 of the fifth heat exchanger 70, and the other end of the fifth hot gas recovery pipeline 71 is connected to the other end of the third hot side pipeline 502 of the third heat exchanger 50 (as shown in fig. 1 to 3). The dust removing device 80 is connected to a dust removing air inlet pipeline 81 and a dust removing air outlet pipeline 82, one end of the dust removing air inlet pipeline 81 is connected to the dust removing device 80, the other end of the dust removing air inlet pipeline 80 is connected to the other end of the fifth hot side pipeline 702 of the fifth heat exchanger 70, one end of the dust removing air outlet pipeline 82 is connected to the dust removing device 80, and the other end of the dust removing air outlet pipeline 82 is connected to the exhaust gas inlet pipeline 21. In addition, a windmill 821 is provided on the dust exhaust gas outlet pipeline 82 so as to push the gas in the dust exhaust gas outlet pipeline 82 to the waste gas inlet pipeline 21. Thus, the gas burned in the direct-fired incinerator 10 can be transferred from the third hot-side pipe 502 of the third heat exchanger 50 to the fifth hot-side pipe 702 of the fifth heat exchanger 70 through the fifth hot-gas recovery pipe 71 for heat recovery, and then transferred into the dust removing device 80 through the dust removing air intake pipe 81 for dust or Silica (SiO) dust or silica2) After the separation of oxides, the gas output from the dust removing device 80 is finally conveyed to the waste gas inlet pipeline 21, so that the combusted gas can enter the adsorption region 201 of the adsorption rotating wheel 20 for recycling, and is not discharged through the chimney 90, the discharge amount of the chimney 90 can be reduced, and the treatment efficiency of the organic waste gas can be improved.
Finally, the fifth heat exchanger is connected to the chimney 90, a chimney exhaust pipe 91 is disposed on the chimney 90, one end of the chimney exhaust pipe 91 is connected to the chimney 90 (as shown in fig. 1 to 3), and the other end of the chimney exhaust pipe 91 is connected to the other end of the fifth cold-side pipe 701 of the fifth heat exchanger 70. The purified gas discharged through the purified gas discharging pipe 22 can enter the fifth cold-side pipe 701 of the fifth heat exchanger 70 for heat exchange, and then is transported to the stack 90 through the stack discharging pipe 91 for discharging. In addition, a windmill 221 is provided on the clean gas discharge line 22 in order to push the gas in the clean gas discharge line 22 towards the fifth cold-side line 701 of the fifth heat exchanger 70.
The second embodiment of the present invention is a direct-fired backflow high-efficiency organic waste gas treatment system, which is mainly provided with a direct-fired incinerator 10, an adsorption rotating wheel 20, a first heat exchanger 30, a second heat exchanger 40, a third heat exchanger 50, a fourth heat exchanger 60, a fifth heat exchanger 70, a dust-removing device 80 and a chimney 90 (as shown in fig. 4 to 6), wherein the first heat exchanger 30 is provided with a first cold-side pipeline 301 and a first hot-side pipeline 302, the second heat exchanger 40 is provided with a second cold-side pipeline 401 and a second hot-side pipeline 402, the third heat exchanger 50 is provided with a third cold-side pipeline 501 and a third hot-side pipeline 502, the fourth heat exchanger 60 is provided with a fourth cold-side pipeline 601 and a fourth hot-side pipeline 602, the fifth heat exchanger 70 is provided with a fifth cold-side pipeline 701 and a fifth hot-side pipeline 702, and the dust-removing device 80 is a bag-type dust remover, Any one of an electric bag type composite dust collector, an inertial dust collector, an electrostatic dust collector, a centrifugal dust collector, a filter cartridge type pulse dust collector, a pulse bag type dust collector, a pulse filter element dust collector, a pulse blowing bag type dust collector, a wet type electrostatic dust collector, a water film dust collector, a Venturi tube dust collector, a cyclone separator, a flue dust collector, a multi-layer dust collector, a negative pressure back blowing filter bag dust collector, a low pressure long bag pulse dust collector, a horizontal type electrostatic dust collector, a non-power dust collector, a charged water mist dust collector, a multi-tube cyclone dust collector or an explosion-proof dust collector, in addition, the direct-fired incinerator (TO)10 is provided with an air inlet 11 and an air outlet 12, and a furnace end and a hearth are arranged in the direct-fired incinerator (TO)10, so that the organic waste gas can enter the furnace end from the air inlet 11 for combustion, and the combusted gas can pass through the hearth and be discharged from the air outlet 12.
The adsorption rotor 20 is a zeolite concentration rotor or a concentration rotor made of other materials, and the adsorption rotor 20 is provided with an adsorption region 201, a cooling region 202 and a desorption region 203, the adsorption rotor 20 is provided with a waste gas inlet pipeline 21, a clean gas discharge pipeline 22, a cooling gas inlet pipeline 23, a cooling gas delivery pipeline 24, a hot gas delivery pipeline 25 and a desorption concentration waste gas pipeline 26 (as shown in fig. 4 to fig. 6), and the other end of the waste gas inlet pipeline 21 is connected to one side of the adsorption region 201 of the adsorption rotor 20, so that the adsorption region 201 of the adsorption rotor 20 can adsorb the waste gas in the waste gas inlet pipeline 21, and one end of the clean gas discharge pipeline 22 is connected to the other side of the adsorption region 201 of the adsorption rotor 20, so that the waste gas is purified by the adsorption region 201 of the adsorption rotor 20 and then is delivered by the clean gas discharge pipeline 22.
In addition, one end of the cooling air inlet pipe 23 is connected to one side of the cooling area 202 of the sorption rotor 20, and the cooling air inlet pipe 23 has two embodiments, wherein the first embodiment is that the cooling air inlet pipe 23 is used for entering external air (as shown in fig. 4 and 5), and the external air is fresh air, so that the external air is used for conveying the external air into the cooling area 202 of the sorption rotor 20 for cooling, and the second embodiment is that a gas bypass pipe 231 (as shown in fig. 6) is provided on the cooling air inlet pipe 23, one end of the gas bypass pipe 231 is connected to the cooling air inlet pipe 23, and the other end of the gas bypass pipe 231 is connected to the exhaust gas inlet pipe 21, so that part of the exhaust gas is conveyed into the cooling area 202 of the sorption rotor 20 for cooling through the gas bypass pipe 21.
In addition, one end of the cooling gas conveying pipeline 24 is connected to the other side of the cooling region 202 of the adsorption rotor 20, the other end of the cooling gas conveying pipeline 24 is connected to one end of the second cold-side pipeline 401 of the second heat exchanger 40, so as to convey the cooling gas in the cooling gas conveying pipeline 24 into the second heat exchanger 40 for heat exchange (as shown in fig. 4 to 6), the other end of the second cold-side pipeline 401 of the second heat exchanger 40 is connected to the other end of the hot gas conveying pipeline 25, one end of the hot gas conveying pipeline 25 is connected to the other side of the desorption region 203 of the adsorption rotor 20, one side of the desorption region 203 of the adsorption rotor 20 is connected to one end of the desorption concentrated gas pipeline 26, so that the hot gas lifted by the second heat exchanger 40 can be conveyed to the desorption region 203 of the adsorption rotor 20 for desorption through the hot gas conveying pipeline 25, and the desorption concentrated gas desorbed at high temperature can be transported through the desorption concentrated gas pipeline 26.
In addition, in the first embodiment of the present invention, a proportional damper is provided between the cooling gas delivery pipeline 24 and the hot gas delivery pipeline 25, and the proportional damper has two implementation designs, wherein the first implementation design is to provide a communication pipeline 27 between the cooling gas delivery pipeline 24 and the hot gas delivery pipeline 25, and the communication pipeline 27 is provided with a communication control valve 271, and the hot gas delivery pipeline 25 is provided with a hot gas control valve 251 (as shown in fig. 5), and the proportional damper is formed by the communication control valve 271 and the hot gas control valve 251, and the second implementation design is to provide a communication pipeline 27 between the cooling gas delivery pipeline 24 and the hot gas delivery pipeline 25, and the communication pipeline 27 is provided with a communication control valve 271, and the cooling gas delivery pipeline 24 is provided with a cooling control valve 241 (as shown in fig. 6), and a proportional damper is formed by the communication control valve 271 and the cooling control valve 241, so that the magnitude of the wind force can be adjusted and controlled regardless of the proportional damper designed by the communication control valve 271 and the hot gas control valve 251 or the proportional damper designed by the communication control valve 271 and the cooling control valve 241, and the temperature in the hot gas delivery pipeline 25 can be kept at a certain high temperature to be supplied to the desorption region 203 of the adsorption rotor 20.
Furthermore, the fourth heat exchanger 60 is connected to a fourth desorption concentrated gas transportation pipeline 61 and a fourth hot gas recovery pipeline 62, one end of the fourth cold-side pipeline 601 is connected to the other end of the desorption concentrated gas pipeline 26, one end of the fourth desorption concentrated gas transportation pipeline 61 is connected to the other end of the fourth cold-side pipeline 601 (as shown in fig. 4 to 6), the other end of the fourth desorption concentrated gas transportation pipeline 61 is connected to one end of the third cold-side pipeline 501 of the third heat exchanger 50, one end of the fourth hot gas recovery pipeline 62 is connected to one end of the fourth hot-side pipeline 602 of the fourth heat exchanger 60, and the other end of the fourth hot gas recovery pipeline 62 is connected to the other end of the third hot-side pipeline 502 of the third heat exchanger 50. Thus, the concentrated desorption gas desorbed from the desorption region 203 of the adsorption rotor 20 can be transferred to the fourth cold-side pipe 601 of the fourth heat exchanger 60 through the concentrated desorption gas pipe 26 for heat exchange, and further transferred to the third cold-side pipe 501 of the third heat exchanger 50 through the fourth concentrated desorption gas pipe 61 for heat exchange.
In addition, the third heat exchanger 50 is connected to a third desorption concentrated gas transportation pipeline 51 and a third hot gas recovery pipeline 52, one end of the third desorption concentrated gas transportation pipeline 51 is connected to the other end of the third cold-side pipeline 501 of the third heat exchanger 50 (as shown in fig. 4 to 6), the other end of the third desorption concentrated gas transportation pipeline 51 is connected to one end of the first cold-side pipeline 301 of the first heat exchanger 30, one end of the third hot gas recovery pipeline 52 is connected to one end of the third hot-side pipeline 502 of the third heat exchanger 50, and the other end of the third hot gas recovery pipeline 52 is connected to the other end of the second hot-side pipeline 402 of the second heat exchanger 40. Thereby, the desorption concentrated gas is transferred to the first cold-side pipe 301 of the first heat exchanger 30 through the third desorption concentrated gas transfer pipe 51 to perform heat exchange.
In addition, the first heat exchanger 30 is connected to a first hot gas recycling pipeline 31, a first incinerating hot gas recycling pipeline 32 and a first desorption concentrated gas delivery pipeline 33, wherein one end of the first incineration hot gas recovery pipe 32 is connected to one end of the first hot side pipe 302 of the first heat exchanger 30, the other end of the first incineration hot gas recovery line 32 is connected to the gas outlet 11 of the direct combustion incinerator 10 (as shown in figures 4 to 6), one end of the first hot gas recovery pipe 31 is connected to the other end of the first hot side pipe 302 of the first heat exchanger 30, the other end of the first hot gas recovery pipe 31 is connected to one end of the second hot side pipe 402 of the second heat exchanger 40, one end of the first desorption concentrated gas transfer line 33 is connected to the other end of the first cold-side line 301 of the first heat exchanger 30, the other end of the first desorption concentrated gas delivery line 33 is connected to the gas inlet 12 of the direct-fired incinerator 10. Therefore, the desorption concentrated gas conveyed by the first cold-side pipeline 301 of the first heat exchanger 30 can be conveyed to the gas inlet 11 of the direct-fired incinerator 10 through the first desorption concentrated gas conveying pipeline 33, the gas combusted by the direct-fired incinerator 10 can be conveyed into the first hot-side pipeline 302 of the first heat exchanger 30 through the first incineration hot gas recovery pipeline 32 through the gas outlet 12 for heat recovery, and is transported via the first hot gas recovery line 31 into the second hot side line 402 of the second heat exchanger 40 for heat recovery, and is then transported through the third hot gas recovery line 52 to the third hot side line 502 of the third heat exchanger 50 for heat recovery, and is then transported through the fourth hot gas recovery line 62 to the fourth hot side line 602 of the fourth heat exchanger 60 for heat recovery.
In addition, a fifth hot gas recovery pipeline 71 is connected to the fifth heat exchanger 70, one end of a fifth cold side pipeline 701 of the fifth heat exchanger 70 is connected to the other end of the clean gas discharge pipeline 22, one end of the fifth hot gas recovery pipeline 71 is connected to one end of a fifth hot side pipeline 702 of the fifth heat exchanger 70 (as shown in fig. 4 to 6), and the other end of the fifth hot gas recovery pipeline 71 is connected to the other end of a fourth hot side pipeline 602 of the fourth heat exchanger 60. The dust removing device 80 is connected to a dust removing air inlet pipeline 81 and a dust removing air outlet pipeline 82, one end of the dust removing air inlet pipeline 81 is connected to the dust removing device 80, the other end of the dust removing air inlet pipeline 81 is connected to the other end of the fifth hot side pipeline 702 of the fifth heat exchanger 70, one end of the dust removing air outlet pipeline 82 is connected to the dust removing device 80, and the other end of the dust removing air outlet pipeline 82 is connected to the exhaust gas inlet pipeline 21. In addition, a windmill 821 is arranged on the dust removal air outlet pipeline 82 so as to facilitate the dust removal air outlet pipeThe gas in the line 82 is pushed into the exhaust gas inlet line 21. Thus, the gas burned in the direct-fired incinerator 10 can be transferred from the fourth hot-side pipe 602 of the fourth heat exchanger 60 to the fifth hot-side pipe 702 of the fifth heat exchanger 70 through the fifth hot-gas recovery pipe 71 for heat recovery, and then transferred into the dust removing device 80 through the dust removing air intake pipe 81 for dust or silica ((SiO 2)2) And finally, the gas output by the dust removal device 80 is conveyed to the waste gas inlet pipeline 21, so that the combusted gas can enter the adsorption region 201 of the adsorption rotating wheel 20 for recycling, and is not discharged through the chimney 90, the discharge amount of the chimney 90 can be reduced, and the treatment efficiency of the organic waste gas can be improved.
Finally, the fifth heat exchanger 70 is connected to the stack 90, a stack exhaust pipe 91 is disposed on the stack 90, one end of the stack exhaust pipe 91 is connected to the stack 90, and the other end of the stack exhaust pipe 91 is connected to the other end of the fifth cold-side pipe 701 of the fifth heat exchanger 70 (as shown in fig. 4 to 6). The purified gas discharged through the purified gas discharging pipe 22 can enter the fifth cold-side pipe 701 of the fifth heat exchanger 70 for heat exchange, and then is transported to the stack 90 through the stack discharging pipe 91 for discharging. The clean gas discharge line 22 is furthermore provided with a windmill 221 in order to be able to push the gas in the clean gas discharge line 22 towards the fifth cold-side line 701 of the fifth heat exchanger 70.
It will be apparent to those skilled in the art from this detailed description that the invention can be practiced without the specific details.
Claims (9)
1. A direct-fired, recirculating high-efficiency, organic exhaust gas treatment system, comprising:
a direct-fired incinerator, which is provided with an air inlet and an air outlet;
the adsorption rotating wheel is provided with an adsorption area, a cooling area and a desorption area, the adsorption rotating wheel is connected with a waste gas inlet pipeline, a clean gas discharge pipeline, a cooling gas inlet pipeline, a cooling gas conveying pipeline, a hot gas conveying pipeline and a desorption concentrated gas pipeline, the other end of the waste gas inlet pipeline is connected to one side of the adsorption area of the adsorption rotating wheel, one end of the clean gas discharge pipeline is connected with the other side of the adsorption area of the adsorption rotating wheel, one end of the cooling gas inlet pipeline is connected with one side of the cooling area of the adsorption rotating wheel, one end of the cooling gas conveying pipeline is connected with the other side of the cooling area of the adsorption rotating wheel, one end of the hot gas conveying pipeline is connected with the other side of the desorption area of the adsorption rotating wheel, and one end of the desorption concentrated gas pipeline is connected with one side of the desorption area of the adsorption rotating wheel;
the first heat exchanger is provided with a first cold side pipeline and a first hot side pipeline, the first heat exchanger is connected with a first hot gas recovery pipeline, a first incineration hot gas recovery pipeline and a first desorption concentrated gas conveying pipeline, one end of the first incineration hot gas recovery pipeline is connected with one end of the first hot side pipeline, the other end of the first incineration hot gas recovery pipeline is connected with the gas outlet of the direct-fired incinerator, one end of the first hot gas recovery pipeline is connected with the other end of the first hot side pipeline, one end of the first desorption concentrated gas conveying pipeline is connected with the other end of the first cold side pipeline, and the other end of the first desorption concentrated gas conveying pipeline is connected with the gas inlet of the direct-fired incinerator;
the second heat exchanger is provided with a second cold side pipeline and a second hot side pipeline, the other end of the first hot gas recovery pipeline is connected with one end of the second hot side pipeline, one end of the second cold side pipeline is connected with the other end of the cooling gas conveying pipeline, and the other end of the second cold side pipeline is connected with the other end of the hot gas conveying pipeline;
the third heat exchanger is provided with a third cold side pipeline and a third hot side pipeline, the third heat exchanger is connected with a third desorption concentrated gas conveying pipeline and a third hot gas recovery pipeline, one end of the third cold side pipeline is connected with the other end of the desorption concentrated gas pipeline, one end of the third desorption concentrated gas conveying pipeline is connected with the other end of the third cold side pipeline, the other end of the third desorption concentrated gas conveying pipeline is connected with one end of the first cold side pipeline, one end of the third hot gas recovery pipeline is connected with one end of the third hot side pipeline, and the other end of the third hot gas recovery pipeline is connected with the other end of the second hot side pipeline;
the fifth heat exchanger is provided with a fifth cold side pipeline and a fifth hot side pipeline, the fifth heat exchanger is connected with a fifth hot gas recovery pipeline, one end of the fifth cold side pipeline is connected with the other end of the purified gas discharge pipeline, one end of the fifth hot gas recovery pipeline is connected with one end of the fifth hot side pipeline, and the other end of the fifth hot gas recovery pipeline is connected with the other end of the third hot side pipeline;
the dust removal equipment is connected with a dust removal air inlet pipeline and a dust removal air outlet pipeline, one end of the dust removal air inlet pipeline is connected with the dust removal equipment, the other end of the dust removal air inlet pipeline is connected with the other end of the fifth hot side pipeline, one end of the dust removal air outlet pipeline is connected with the dust removal equipment, and the other end of the dust removal air outlet pipeline is connected with the waste gas inlet pipeline; and
and the chimney is provided with a chimney discharge pipeline, one end of the chimney discharge pipeline is connected with the chimney, and the other end of the chimney discharge pipeline is connected with the other end of the fifth cold side pipeline of the fifth heat exchanger.
2. A direct-fired, recirculating high-efficiency, organic exhaust gas treatment system, comprising:
a direct-fired incinerator, which is provided with an air inlet and an air outlet;
the adsorption rotating wheel is provided with an adsorption area, a cooling area and a desorption area, the adsorption rotating wheel is connected with a waste gas inlet pipeline, a clean gas discharge pipeline, a cooling gas inlet pipeline, a cooling gas conveying pipeline, a hot gas conveying pipeline and a desorption concentrated gas pipeline, the other end of the waste gas inlet pipeline is connected to one side of the adsorption area of the adsorption rotating wheel, one end of the clean gas discharge pipeline is connected with the other side of the adsorption area of the adsorption rotating wheel, one end of the cooling gas inlet pipeline is connected with one side of the cooling area of the adsorption rotating wheel, one end of the cooling gas conveying pipeline is connected with the other side of the cooling area of the adsorption rotating wheel, one end of the hot gas conveying pipeline is connected with the other side of the desorption area of the adsorption rotating wheel, and one end of the desorption concentrated gas pipeline is connected with one side of the desorption area of the adsorption rotating wheel;
the first heat exchanger is provided with a first cold side pipeline and a first hot side pipeline, the first heat exchanger is connected with a first hot gas recovery pipeline, a first incineration hot gas recovery pipeline and a first desorption concentrated gas conveying pipeline, one end of the first incineration hot gas recovery pipeline is connected with one end of the first hot side pipeline, the other end of the first incineration hot gas recovery pipeline is connected with the gas outlet of the direct-fired incinerator, one end of the first hot gas recovery pipeline is connected with the other end of the first hot side pipeline, one end of the first desorption concentrated gas conveying pipeline is connected with the other end of the first cold side pipeline, and the other end of the first desorption concentrated gas conveying pipeline is connected with the gas inlet of the direct-fired incinerator;
the second heat exchanger is provided with a second cold side pipeline and a second hot side pipeline, the other end of the first hot gas recovery pipeline is connected with one end of the second hot side pipeline, one end of the second cold side pipeline is connected with the other end of the cooling gas conveying pipeline, and the other end of the second cold side pipeline is connected with the other end of the hot gas conveying pipeline;
the third heat exchanger is provided with a third cold side pipeline and a third hot side pipeline, the third heat exchanger is connected with a third desorption concentrated gas conveying pipeline and a third hot gas recovery pipeline, one end of the third desorption concentrated gas conveying pipeline is connected with the other end of the third cold side pipeline, the other end of the third desorption concentrated gas conveying pipeline is connected with one end of the first cold side pipeline, one end of the third hot gas recovery pipeline is connected with one end of the third hot side pipeline, and the other end of the third hot gas recovery pipeline is connected with the other end of the second hot side pipeline;
a fourth heat exchanger, which is provided with a fourth cold side pipeline and a fourth hot side pipeline, the fourth heat exchanger is connected with a fourth desorption concentrated gas conveying pipeline and a fourth hot gas recovery pipeline, one end of the fourth cold side pipeline is connected with the other end of the desorption concentrated gas pipeline, one end of the fourth desorption concentrated gas conveying pipeline is connected with the other end of the fourth cold side pipeline, the other end of the fourth desorption concentrated gas conveying pipeline is connected with one end of the third cold side pipeline, one end of the fourth hot gas recovery pipeline is connected with one end of the fourth hot side pipeline, and the other end of the fourth hot gas recovery pipeline is connected with the other end of the third hot side pipeline;
the fifth heat exchanger is provided with a fifth cold side pipeline and a fifth hot side pipeline, the fifth heat exchanger is connected with a fifth hot gas recovery pipeline, one end of the fifth cold side pipeline is connected with the other end of the purified gas discharge pipeline, one end of the fifth hot gas recovery pipeline is connected with one end of the fifth hot side pipeline, and the other end of the fifth hot gas recovery pipeline is connected with the other end of the fourth hot side pipeline;
the dust removal equipment is connected with a dust removal air inlet pipeline and a dust removal air outlet pipeline, one end of the dust removal air inlet pipeline is connected with the dust removal equipment, the other end of the dust removal air inlet pipeline is connected with the other end of the fifth hot side pipeline, one end of the dust removal air outlet pipeline is connected with the dust removal equipment, and the other end of the dust removal air outlet pipeline is connected with the waste gas inlet pipeline; and
and the chimney is provided with a chimney discharge pipeline, one end of the chimney discharge pipeline is connected with the chimney, and the other end of the chimney discharge pipeline is connected with the other end of the fifth cold side pipeline of the fifth heat exchanger.
3. The system as claimed in claim 1 or 2, wherein a communication line is further disposed between the cooling gas delivery line and the hot gas delivery line, the communication line is provided with a communication control valve, the hot gas delivery line is provided with a hot gas control valve, and the communication control valve and the hot gas control valve form a proportional damper.
4. The system as claimed in claim 1 or 2, wherein a communication pipe is further provided between the cooling gas delivery pipe and the hot gas delivery pipe, the communication pipe is provided with a communication control valve, the cooling gas delivery pipe is provided with a cooling control valve, and the communication control valve and the cooling control valve form a proportional damper.
5. The direct-fired reflux high efficiency organic waste gas treatment system according to claim 1 or 2, wherein the dust removal equipment is further any one of a bag type dust collector, an electric bag type composite dust collector, an inertial dust collector, an electrostatic dust collector, a centrifugal dust collector, a cartridge type pulse dust collector, a pulse bag type dust collector, a pulse filter element dust collector, a pulse blowing bag type dust collector, a wet type electrostatic dust collector, a water film dust collector, a venturi tube dust collector, a cyclone separator, a flue dust collector, a multilayer dust collector, a negative pressure back-blowing filter bag dust collector, a low pressure long bag pulse dust collector, a horizontal type electrostatic dust collector, a non-dynamic dust collector, a charged water mist dust collector, a multi-tube cyclone dust collector or an explosion-proof dust collector.
6. The system of claim 1 or 2, wherein the cooling air intake conduit further delivers outside air to the cooling zone of the sorption rotor, and the outside air is fresh air.
7. The direct-fired reflux high efficiency organic waste gas treatment system according to claim 1 or 2, wherein the cooling gas inlet pipe is further provided with a gas bypass pipe, one end of the gas bypass pipe is connected with the cooling gas inlet pipe, and the other end of the gas bypass pipe is connected with the waste gas inlet pipe.
8. The system of claim 1 or 2, wherein the clean gas exhaust pipeline is further provided with a windmill.
9. The system of claim 1 or 2, wherein the dust removal outlet pipeline is further provided with a windmill.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| TW108200977U TWM579063U (en) | 2019-01-21 | 2019-01-21 | Thermal oxidation backflow high-efficiency organic waste gas processing system |
| TW108200977 | 2019-01-21 |
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| CN210511720U true CN210511720U (en) | 2020-05-12 |
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| CN201920253816.3U Active CN210511720U (en) | 2019-01-21 | 2019-02-28 | Direct-fired backflow high-efficiency organic waste gas treatment system |
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| TW (1) | TWM579063U (en) |
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| TWI722522B (en) * | 2019-08-07 | 2021-03-21 | 華懋科技股份有限公司 | Heat storage reflux high-efficiency organic waste gas treatment system and method |
| TWI741341B (en) * | 2019-08-07 | 2021-10-01 | 華懋科技股份有限公司 | Organic waste gas concentrated heat storage combustion backflow system and method |
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2019
- 2019-01-21 TW TW108200977U patent/TWM579063U/en unknown
- 2019-02-28 CN CN201920253816.3U patent/CN210511720U/en active Active
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