CN112344352A - Heat accumulation backflow high-efficiency organic waste gas treatment system and method - Google Patents
Heat accumulation backflow high-efficiency organic waste gas treatment system and method Download PDFInfo
- Publication number
- CN112344352A CN112344352A CN201910929242.1A CN201910929242A CN112344352A CN 112344352 A CN112344352 A CN 112344352A CN 201910929242 A CN201910929242 A CN 201910929242A CN 112344352 A CN112344352 A CN 112344352A
- Authority
- CN
- China
- Prior art keywords
- pipeline
- gas
- dust collector
- cooling
- hot
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 239000007789 gas Substances 0.000 title claims abstract description 555
- 239000010815 organic waste Substances 0.000 title claims abstract description 54
- 238000009825 accumulation Methods 0.000 title claims abstract description 42
- 238000000034 method Methods 0.000 title claims abstract description 37
- 238000011084 recovery Methods 0.000 claims abstract description 131
- 238000001179 sorption measurement Methods 0.000 claims abstract description 127
- 238000010438 heat treatment Methods 0.000 claims abstract description 68
- 239000002912 waste gas Substances 0.000 claims abstract description 34
- 239000000428 dust Substances 0.000 claims description 243
- 230000001172 regenerating effect Effects 0.000 claims description 168
- 238000001816 cooling Methods 0.000 claims description 145
- 238000003795 desorption Methods 0.000 claims description 107
- 239000000112 cooling gas Substances 0.000 claims description 75
- 238000004064 recycling Methods 0.000 claims description 71
- 238000004891 communication Methods 0.000 claims description 58
- 238000010992 reflux Methods 0.000 claims description 54
- 239000007800 oxidant agent Substances 0.000 claims description 48
- 238000010926 purge Methods 0.000 claims description 39
- 230000002000 scavenging effect Effects 0.000 claims description 39
- 238000005338 heat storage Methods 0.000 claims description 32
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 22
- 238000007664 blowing Methods 0.000 claims description 17
- 239000003500 flue dust Substances 0.000 claims description 11
- 239000003595 mist Substances 0.000 claims description 11
- 239000002131 composite material Substances 0.000 claims description 2
- 238000003672 processing method Methods 0.000 claims description 2
- 150000001875 compounds Chemical class 0.000 claims 4
- 239000012141 concentrate Substances 0.000 claims 2
- 238000002485 combustion reaction Methods 0.000 description 19
- 238000013461 design Methods 0.000 description 17
- 238000010586 diagram Methods 0.000 description 9
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 8
- 238000003860 storage Methods 0.000 description 7
- 239000012716 precipitator Substances 0.000 description 6
- 239000000498 cooling water Substances 0.000 description 5
- 239000000446 fuel Substances 0.000 description 4
- 239000002737 fuel gas Substances 0.000 description 4
- 239000007788 liquid Substances 0.000 description 4
- 239000000377 silicon dioxide Substances 0.000 description 4
- 125000004122 cyclic group Chemical group 0.000 description 3
- 238000005086 pumping Methods 0.000 description 3
- 239000004065 semiconductor Substances 0.000 description 3
- 229910021536 Zeolite Inorganic materials 0.000 description 2
- 230000001276 controlling effect Effects 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
- 238000007599 discharging Methods 0.000 description 2
- 239000012717 electrostatic precipitator Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000010457 zeolite Substances 0.000 description 2
- 238000003915 air pollution Methods 0.000 description 1
- 238000001914 filtration 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
Images
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
- F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
- F23G5/44—Details; Accessories
- F23G5/46—Recuperation of heat
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
- F23J15/022—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material for removing solid particulate material from the gasflow
- F23J15/025—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material for removing solid particulate material from the gasflow using filters
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/06—Arrangements of devices for treating smoke or fumes of coolers
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/30—Technologies for a more efficient combustion or heat usage
Abstract
A heat accumulation backflow high-efficiency organic waste gas treatment system and a method thereof are mainly characterized in that hot gas of a heating chamber of a heat accumulation type incinerator is supplied to a heat exchanger for heat exchange, and the exhaust gas of the heat accumulation type incinerator is subjected to heat exchange through a recovery heat exchanger or a cooler and is conveyed to a waste gas inlet pipeline after being subjected to heat exchange or cooled, so that the combusted gas enters an adsorption area of an adsorption rotating wheel and is not discharged through a chimney, the discharge amount of the chimney is reduced, and the treatment efficiency of organic waste gas is improved.
Description
Technical Field
The invention relates to a heat accumulation backflow high-efficiency organic waste gas treatment system and a method thereof, in particular to an organic waste gas treatment system or similar equipment which is used for enabling combusted gas to enter an adsorption area of an adsorption rotating wheel for cyclic utilization, does not need to be discharged through a chimney, improves the treatment efficiency of organic waste gas and is suitable for semiconductor industry, photoelectric industry or chemical related industry.
Background
At present, volatile organic gases ((VOC)) are generated in the manufacturing process of semiconductor industry or photovoltaic industry, and therefore, processing equipment for processing the volatile organic gases ((VOC)) is installed in each factory to prevent the volatile organic gases ((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.
Therefore, in view of the above-mentioned shortcomings, the present inventors have expected to provide a system and a method for efficiently treating organic waste gas by heat accumulation and recirculation, which can be easily assembled by a user, so as to provide convenience to the user by making an extensive study on thinking and design.
Disclosure of Invention
The main objective of the present invention is to provide a system and method for efficiently treating organic waste gas by regenerative thermal reflux, wherein the hot gas in the heating chamber of the regenerative thermal incinerator is supplied to the heat exchanger for heat exchange, and the exhaust gas of the regenerative thermal incinerator is subjected to heat exchange by the recovery heat exchanger or the cooler, and is then conveyed to the waste gas inlet pipeline after heat exchange or cooling, so that the combusted gas enters the adsorption region of the adsorption rotating wheel and is not discharged through the chimney, thereby reducing the discharge amount of the chimney, improving the treatment efficiency of the organic waste gas, and further increasing the overall practicability.
Another objective of the present invention is to provide a regenerative thermal reflux high efficiency organic waste gas treatment system and method thereof, wherein hot gas in a heating chamber of the regenerative thermal oxidizer is output from a hot gas outlet of the heating chamber, and is delivered into a hot side pipeline of the heat exchanger through a regenerative gas recycling pipeline connected to the hot gas outlet of the heating chamber, and is delivered into a desorption concentrated gas pipeline through the hot gas recycling pipeline connected to one end of the hot side pipeline of the heat exchanger, so that the gas after heat exchange by the heat exchanger is returned to the regenerative thermal oxidizer through the desorption concentrated gas pipeline for combustion, thereby achieving recycling efficiency and increasing the overall usability.
A further object of the present invention is to provide a regenerative thermal oxidizer and a method thereof, wherein when the regenerative thermal oxidizer is a rotary regenerative thermal oxidizer or when at least three regenerative beds are provided in the regenerative thermal oxidizer, the regenerative thermal oxidizer is provided with a scavenging (purge) pipeline, the other end of the scavenging (purge) pipeline is connected to the heating chamber, hot air in the heating chamber of the regenerative thermal oxidizer is output from a hot air outlet of the heating chamber and is delivered to a hot side pipeline of the heat exchanger through a regenerative air recycling pipeline connected to the hot air outlet of the heating chamber, and is delivered to a scavenging (purge) pipeline through the hot air recycling pipeline connected to one end of the hot side pipeline of the heat exchanger, and the air after heat exchange through the heat exchanger is returned to the heating chamber through the scavenging (purge) pipeline, the recycling efficiency is achieved, and the overall operability is improved.
For a better understanding of the nature, features and aspects of the present invention, reference should be made to the following detailed description of the invention, taken in conjunction with the accompanying drawings, which are provided for purposes of illustration and description only and are not intended to be limiting.
Drawings
FIG. 1 is a flow chart of the main steps of a first embodiment of the present invention;
FIG. 2 is a schematic diagram of a first embodiment of the present invention;
FIG. 3 is a schematic view of a first configuration of a second thermal storage bed according to a first embodiment of the present invention;
FIG. 4 is a schematic diagram of a second configuration of a second thermal storage bed according to the first embodiment of the invention;
FIG. 5 is a flow diagram of a first architecture of a three thermal storage bed according to a first embodiment of the present invention;
FIG. 6 is a schematic diagram of a second architecture of a triple heat storage bed according to the first embodiment of the invention;
FIG. 7 is a flow chart of the main steps of a second embodiment of the present invention;
FIG. 8 is a schematic diagram of a second embodiment of the present invention;
FIG. 9 is a schematic view of a first configuration of a second thermal storage bed according to a second embodiment of the present invention;
FIG. 10 is a schematic diagram of a second configuration of a second thermal storage bed according to a second embodiment of the invention;
FIG. 11 is a flow diagram of a first architecture of a three thermal storage bed according to a second embodiment of the present invention;
FIG. 12 is a schematic diagram of a second configuration of a triple thermal storage bed according to a second embodiment of the present invention.
In the above drawings, the reference numerals have the following meanings:
A. one side B and the other side
10. Heat accumulating type incinerator 101 and heat accumulating bed
101. First and second heat storage beds 102 and 102
103. Third heat storage bed 11, heating chamber
111. Hot gas outlet 12, air inlet pipeline
13. Gas outlet pipeline 14 and scavenging pipeline
20. Adsorption rotating wheel 201 and adsorption area
202. Cooling zone 203, desorption zone
21. Exhaust gas inlet line 22 and clean gas discharge line
221. Fan 222 and clean gas bypass pipeline
2221. Clean gas bypass control valve 23 and cooling gas inlet pipeline
231. Gas bypass pipeline 24 and cooling gas conveying pipeline
241. Cooling air control valve 25 and hot gas delivery line
251. Hot gas control valve 26, desorption concentration waste gas pipeline
261. Blower 27, communication pipe
271. Communication control valve 30 and heat exchanger
301. Cold side duct 302, hot side duct
31. Hot gas recovery line 32 and heat storage gas recovery line
40. Return heat exchanger 401, return cold side piping
402. Return hot side pipeline 41 and return hot gas recovery pipeline
42. Return recovery pipeline 421 and fan
50. Cooling device
51. Cooling reflux hot gas recovery pipeline
52. Cooling reflux recovery pipeline 521 and fan
53. Cooling water pipeline 60 and dust removing equipment
70. Chimney 71, chimney exhaust line
711. Fan blower
S100, adsorption S110 in adsorption zone, and cooling in cooling zone
S120, desorption S130 in desorption area, and heat storage gas conveying
S140, recovering and conveying the exhaust gas S150 through a return recovery pipeline
S200, adsorption in adsorption zone S210, cooling in cooling zone
S220, desorption in desorption area S230, and heat storage gas conveying
S240, exhaust gas recovery and transportation
S250, cooling, refluxing and recycling pipeline
Detailed Description
Referring to fig. 1 to 12, schematic diagrams of embodiments of the present invention are shown, and a preferred embodiment of the heat-accumulation backflow high-efficiency organic waste gas treatment system and method of the present invention is applied to a volatile organic waste gas treatment system or similar devices in the semiconductor industry, the photoelectric industry, or the chemical industry.
The heat-accumulating backflow high-efficiency organic waste gas treatment system according to the first embodiment of the present invention mainly includes a heat-accumulating incinerator (RTO)10, an adsorbing rotating wheel 20, a heat exchanger 30 and a backflow heat exchanger 40 (as shown in fig. 2 to 6), wherein the heat exchanger 30 has a cold-side pipeline 301 and a hot-side pipeline 302, the heat exchanger 30 is connected to a hot-gas recycling pipeline 31 and a heat-accumulating gas recycling pipeline 32, the backflow heat exchanger 40 has a backflow cold-side pipeline 401 and a backflow hot-side pipeline 402, the backflow heat exchanger 40 is connected to a backflow hot-gas recycling pipeline 41 and a backflow recycling pipeline 42, the heat-accumulating incinerator (RTO)10 is provided with a heat-accumulating bed 101, the heat-accumulating bed 101 may have two heat-accumulating beds (as shown in fig. 2 to 4), three heat-accumulating beds (as shown in fig. 5 and fig. 6), four heat-accumulating beds (not shown in the figures), or five heat-accumulating beds (not shown, the Regenerative Thermal Oxidizer (RTO)10 has a heating chamber 11, at least one air inlet duct 12 and at least one air outlet duct 13, and the heating chamber 11 has a hot air outlet 111 (as shown in fig. 2 to 6). In addition, the regenerative thermal oxidizer ((RTO))10 may be a rotary regenerative thermal oxidizer ((not shown)).
When the Regenerative Thermal Oxidizer (RTO)10 of the present invention has a heating chamber 11 and at least three regenerative beds 101 (as shown in fig. 5 and 6), the three regenerative beds 101 are respectively provided as a first regenerative bed 1011, a second regenerative bed 1012 and a third regenerative bed 1013, the first regenerative bed 1011, the second regenerative bed 1012 and the third regenerative bed 1013 are all communicated with the heating chamber 11, and the regenerative bed 101 is used for storing and releasing heat to recover the heat energy of the high-temperature exhaust gas for preheating the low-temperature intake air, and the first regenerative bed 1011, the second regenerative bed 1012 or the third regenerative bed 1013 are used by being switched with each other. In addition, the heating chamber 11 of the regenerative thermal oxidizer ((RTO))10 is provided with a burner (as shown in fig. 2 to 6) which introduces fuel gas or fuel liquid for combustion and transfers hot gas during combustion to the heating chamber 11 of the Regenerative Thermal Oxidizer (RTO)10 for use, and the burner is provided with an air pipeline which is provided with a fan, and air in the air pipeline is pushed into the burner by the fan to assist combustion and generate temperature rise.
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. 2 to fig. 6), and the other end of the waste gas inlet pipeline 21 is connected to one side a of the adsorption region 201 of the adsorption rotor 20, so that the adsorption region 201 of the adsorption rotor 20 adsorbs 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 B 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 a 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. 3 and 5), 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 the cooling air inlet pipe 23 is provided with a gas bypass pipe 231 (as shown in fig. 4 and 6), 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 202 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 B 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 cold side pipeline 301 of the heat exchanger 30, so as to convey the cooling gas in the cooling gas conveying pipeline 24 into the heat exchanger 30 for heat exchange (as shown in fig. 2 to 6), the other end of the cold side pipeline 301 of the heat exchanger 30 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 B of the desorption region 203 of the adsorption rotor 20, one side a of the desorption region 203 of the adsorption rotor 20 is connected to one end of the desorption concentrated gas pipeline 26 (as shown in fig. 2 to 6), so that the hot gas lifted by the heat exchanger 30 is conveyed to the desorption region 203 of the adsorption rotor 20 through the hot gas conveying pipeline 25 for desorption, and the desorption concentrated gas desorbed at high temperature is transported through the desorption concentrated gas pipeline 26, and the other end of the desorption concentrated gas pipeline 26 is connected with at least one air inlet pipeline 12 of the regenerative incinerator 10, so that the desorption concentrated gas enters the regenerative incinerator 10 to be combusted. In addition, the desorption concentrated gas pipeline 26 is provided with a fan 261 for pumping the desorption concentrated gas in the desorption concentrated gas pipeline 26.
In addition, a proportional damper (as shown in fig. 3 to 6) is disposed 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 that a communication pipeline 27 is disposed between the cooling gas delivery pipeline 24 and the hot gas delivery pipeline 25, and the communication pipeline 27 is disposed with a communication control valve 271, and the hot gas delivery pipeline 25 is disposed with a hot gas control valve 251, 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 that a communication pipeline 27 is disposed between the cooling gas delivery pipeline 24 and the hot gas delivery pipeline 25, and the communication pipeline 27 is disposed with a communication control valve 271, and the cooling gas delivery pipeline 24 is disposed with a cooling control valve 241, and the proportional damper is formed by the communication control valve 271 and the cooling control valve 241, therefore, the air flow can be controlled by adjusting the design of the communication control valve 271 and the hot air control valve 25 or the design of the communication control valve 271 and the cooling control valve 241, so that the temperature in the hot air delivery pipeline 25 can be kept at a certain high temperature for the desorption region 203 of the adsorption rotor 20.
In addition, the heat exchanger 30 is connected to a hot gas recycling line 31 and a hot gas recycling line 32, wherein one end of the hot gas recycling line 32 is connected to the hot gas outlet 111 of the heating chamber 11 of the regenerative incinerator 10 (as shown in fig. 2 to 6), the other end of the hot gas recycling line 32 is connected to the other end of the hot side line 302 of the heat exchanger 30, and one end of the hot gas recycling line 31 is connected to one end of the hot side line 302 of the heat exchanger 30. Therefore, the desorption concentrated gas is delivered to at least one air inlet pipeline 12 of the regenerative incinerator 10 through the desorption concentrated gas delivery pipeline 26, and the gas combusted by the regenerative incinerator 10 is delivered to the hot side pipeline 302 of the heat exchanger 30 for heat recovery through the regenerative gas recovery pipeline 32 from the hot gas outlet 111 of the heating chamber 11, and is delivered through the hot gas recovery pipeline 31.
The above-mentioned hot gas recycling pipeline 31 has two connecting paths, the first path is that the other end of the hot gas recycling pipeline 31 is connected to the desorption concentrated gas pipeline 26 (as shown in fig. 2 to fig. 4), so that the gas that is transported into the hot side pipeline 302 of the heat exchanger 30 by the heat-storage gas recycling pipeline 32 for heat recycling is transported into the desorption concentrated gas pipeline 26 by the hot gas recycling pipeline 31, and then transported into the heat-storage type incinerator 10 for repeated combustion by the desorption concentrated gas pipeline 26, so as to have recycling efficiency.
The second path is when at least three regenerative beds 101 are provided in the regenerative thermal oxidizer 10 or when the regenerative thermal incinerator 10 is a rotary regenerative thermal incinerator (not shown), the regenerative bed 101 of the regenerative thermal oxidizer 10 is provided with a scavenging (purge) line 14 (shown in fig. 5 and 6), and the other end of the scavenging (purge) line 14 is connected to the heating chamber 11, so that when the heat storage bed 101 is not used for the intake air or the exhaust air, the scavenging gas (purge) can be supplied into the heating chamber 11 through the scavenging line 14, and therefore, the other end of the hot gas recovery line 31 is connected to the scavenging ((purge)) line 14, and the gas, which is sent to the hot side line 302 of the heat exchanger 30 through the heat storage gas recovery line 32 and subjected to heat recovery, is sent to the scavenging ((purge)) line 14 through the hot gas recovery line 31 and then sent to the heating chamber 11 through the scavenging ((purge)) line 14.
In addition, the heat-returning heat exchanger 40 is connected to a hot-returning gas recycling pipeline 41 and a hot-returning gas recycling pipeline 42, one end of the cold-returning pipeline 401 of the heat-returning heat exchanger 40 is connected to the other end of the clean gas discharging pipeline 22, one end of the hot-returning pipeline 41 is connected to one end of the hot-returning pipeline 402 of the heat-returning heat exchanger 40, the other end of the hot-returning pipeline 41 is connected to the gas outlet pipeline 13 of the regenerative incinerator 10 (as shown in fig. 2 to 6), one end of the hot-returning pipeline 42 is connected to the other end of the hot-returning pipeline 402 of the heat-returning heat exchanger 40, and the other end of the hot-returning pipeline 42 is connected to the exhaust gas inlet pipeline 21. Furthermore, the hot gas return line 41 and the hot gas return line 42 of the heat return exchanger 40 can be provided with a dust removing device 60 (as shown in fig. 6), or a dust removing device 60 is provided on the hot gas return line 42 of the heat return exchanger 40 (as shown in fig. 3 and 5), or a dust removing device 60 is provided on the hot gas return line 41 of the heat return exchanger 40 (as shown in fig. 4), so that the gas passing through the hot gas return line 41 or the gas passing through the hot gas return line 42 can be filtered by the dust removing device 60, wherein the dust removing device 60 is a bag filter, an electric bag filter, an inertial filter, an electrostatic precipitator, a centrifugal precipitator, a filter cartridge pulse precipitator, a pulse bag filter, a pulse filter cartridge precipitator, a pulse filter, a vacuum cleaner, pulse blowing bag type dust collector, wet type electric dust collector, wet type electrostatic dust collector, water film dust collector, Venturi tube dust collector, cyclone separator, flue dust collector, multilayer dust collector, negative pressure back-blowing filter bag dust collector, low pressure long bag pulse dust collector, horizontal type electrostatic dust collector, vacuum pump,Any one of a unpowered dust collector, a charged water mist dust collector, a multi-cyclone dust collector and an explosion-proof dust collector, and a blower 421 (shown in fig. 2 to 6) is provided in the return recovery pipeline 42 of the return heat exchanger 40 to push the gas in the return recovery pipeline 42 into the exhaust gas inlet pipeline 21. Thus, the gas burned in the regenerative thermal oxidizer 10 is transferred to the hot-side return pipe 402 of the return heat exchanger 40 through the hot-gas return pipe 41 for heat recovery, and then transferred to the dust removing device 60 through the return recovery pipe 42 for dust or silica ((SiO) oxide)2) And finally, the gas output by the dust removal device 60 is conveyed into the waste gas inlet pipeline 21, so that the combusted gas enters the adsorption area 201 of the adsorption rotating wheel 20 and is not discharged through the chimney 70, the discharge amount of the chimney 70 is reduced, and the treatment efficiency of the organic waste gas is improved.
The heat-returning exchanger 40 is connected to a chimney 70, the chimney 70 is provided with a chimney discharge pipe 71 (as shown in fig. 2 to fig. 6), one end of the chimney discharge pipe 71 is connected to the chimney 70, the other end of the chimney discharge pipe 71 is connected to the other end of the return cold-side pipe 401 of the heat-returning exchanger 40, so that the purified gas discharged through the clean gas discharge pipe 22 enters the return cold-side pipe 401 of the heat-returning exchanger 40 for heat exchange, and is then conveyed to the chimney 70 through the chimney discharge pipe 71 for discharge, and the chimney discharge pipe 71 is provided with a fan 711 (as shown in fig. 4 and fig. 6) for pushing the gas in the chimney discharge pipe 71 into the chimney 70. The clean gas discharge line 22 is further provided with a blower 221 (see fig. 3 to 6) to push the gas in the clean gas discharge line 22 towards the return cold side line 401 of the return heat exchanger 40. A purified gas bypass line 222 is disposed beside the purified gas discharge line 22, one end of the purified gas bypass line 222 is connected to the purified gas discharge line 22 (as shown in fig. 2 to 6), and the other end of the purified gas bypass line 222 is connected to the chimney discharge line 71, so that when the purified gas discharged from the purified gas discharge line 22 is transported, the purified gas enters the reflux cold-side line 401 of the reflux heat exchanger 40 for heat exchange, and is bypassed by the purified gas bypass line 222 connected to the purified gas discharge line 22, so that a part of the purified gas directly flows to the chimney discharge line 71 and is discharged through the chimney 70. In addition, the net gas bypass line 222 is provided with a net gas bypass control valve 2221, so as to adjust the air volume of the purified gas delivered from the net gas discharge line 22 through the net gas bypass control valve 2221, thereby achieving the adjusting and controlling effect.
A first embodiment of the present invention provides a method for treating organic waste gas with high efficiency by heat accumulation backflow, which is mainly used for the organic waste gas treatment system, and comprises a heat accumulation type incinerator (RTO)10, an adsorption rotating wheel 20, a heat exchanger 30 and a heat recovery heat exchanger 40 (as shown in fig. 2 to 6), wherein the heat exchanger 30 is provided with a cold side pipeline 301 and a hot side pipeline 302, the heat exchanger 30 is connected with a hot gas recovery pipeline 31 and a heat accumulation gas recovery pipeline 32, the heat recovery heat exchanger 40 is provided with a backflow cold side pipeline 401 and a hot side backflow pipeline 402, the heat recovery heat exchanger 40 is connected with a backflow hot gas recovery pipeline 41 and a backflow recovery pipeline 42, a heat accumulation bed 101 is arranged in the heat accumulation type incinerator (RTO)10, and the heat accumulation bed 101 may be provided with two heat accumulation beds (as shown in fig. 2 to 4), three heat accumulation beds (as shown in fig. 5 and 6), Four regenerative beds (not shown) or five regenerative beds (not shown), the Regenerative Thermal Oxidizer (RTO)10 has a heating chamber 11, at least one inlet duct 12 and at least one outlet duct 13, and the heating chamber 11 has a hot gas outlet 111 (see fig. 2 to 3). In addition, the regenerative thermal oxidizer ((RTO))10 may be a rotary regenerative thermal oxidizer ((not shown)).
When the Regenerative Thermal Oxidizer (RTO)10 of the present invention has a heating chamber 11 and at least three regenerative beds 101 (as shown in fig. 5 and 6), the three regenerative beds 101 are respectively provided as a first regenerative bed 1011, a second regenerative bed 1012 and a third regenerative bed 1013, the first regenerative bed 1011, the second regenerative bed 1012 and the third regenerative bed 1013 are all communicated with the heating chamber 11, and the regenerative bed 101 is used for storing and releasing heat to recover the heat energy of the high-temperature exhaust gas for preheating the low-temperature intake air, and the first regenerative bed 1011, the second regenerative bed 1012 or the third regenerative bed 1013 are used by being switched with each other. In addition, the heating chamber 11 of the regenerative thermal oxidizer ((RTO))10 is provided with a burner (as shown in fig. 2 to 6) which introduces fuel gas or fuel liquid for combustion and transfers hot gas during combustion to the heating chamber 11 of the Regenerative Thermal Oxidizer (RTO)10 for use, and the burner is provided with an air pipeline which is provided with a fan, and air in the air pipeline is pushed into the burner by the fan to assist combustion and generate temperature rise.
The main steps of the treatment method (as shown in fig. 1) include: step S100 adsorption in adsorption zone: the exhaust gas is fed to one side a of the adsorption region 201 of the adsorption rotor 20 through the other end of the exhaust gas inlet line 21 to be adsorbed, and the adsorbed gas is then fed to one end of the return cold-side line 401 of the return heat exchanger 40 through the other end of the net gas discharge line 22. After the step S100 is completed, the next step S110 is performed.
In the above step S100, the heat-returning exchanger 40 is connected to a chimney 70, the chimney 70 is provided with a chimney discharge pipe 71 (as shown in fig. 2 to fig. 6), one end of the chimney discharge pipe 71 is connected to the chimney 70, the other end of the chimney discharge pipe 71 is connected to the other end of the return cold-side pipe 401 of the heat-returning exchanger 40, so that the purified gas discharged through the clean gas discharge pipe 22 enters the return cold-side pipe 401 of the heat-returning exchanger 40 for heat exchange, and is then transported to the chimney 70 through the chimney discharge pipe 71 for discharge, and the chimney discharge pipe 71 is provided with a fan 711 (as shown in fig. 4 and fig. 6) for pushing the gas in the chimney discharge pipe 71 into the chimney 70. The clean gas discharge line 22 is further provided with a blower 221 (see fig. 3 to 6) to push the gas in the clean gas discharge line 22 towards the return cold side line 401 of the return heat exchanger 40. A purified gas bypass line 222 (as shown in fig. 3 to 6) is disposed beside the purified gas discharge line 22, one end of the purified gas bypass line 222 is connected to the purified gas discharge line 22, and the other end of the purified gas bypass line 222 is connected to the chimney discharge line 71, so that when the purified gas discharged from the purified gas discharge line 22 is transported, the purified gas enters the reflux cold-side line 401 of the reflux heat exchanger 40 for heat exchange, and is bypassed by the purified gas bypass line 222 connected to the purified gas discharge line 22, so that a part of the purified gas directly flows to the chimney discharge line 71 and is discharged through the chimney 70. In addition, the net gas bypass line 222 is provided with a net gas bypass control valve 2221 (as shown in fig. 3 to 6), so as to adjust the air volume of the purified gas delivered from the net gas discharge line 22 through the net gas bypass control valve 2221, thereby achieving the adjusting and controlling effect.
In addition, the next step S110 cooling zone cooling: the cooling gas is supplied to the cooling zone 202 of the sorption rotor 20 through the other end of the cooling gas inlet conduit 23 for cooling, and the cooling gas passing through the cooling zone 202 is supplied to one end of the cold-side conduit 301 of the heat exchanger 30 through the other end of the cooling gas supply conduit 24. After the step S110 is completed, the next step S120 is performed.
Wherein one end of the cooling air inlet pipe 23 is connected to one side a of the cooling zone 202 of the sorption rotor 20 in the above-mentioned step S110, and the cooling air inlet pipe 23 has two embodiments, in the first embodiment, the cooling air inlet pipe 23 is used for the inlet of external air (as shown in fig. 3 and 5), the external air is fresh air, so that the external air is used for conveying into the cooling zone 202 of the adsorption runner 20 for cooling, in a second embodiment, the cooling air inlet pipe 23 is provided with a gas bypass pipe 231 (as shown in figures 4 and 6), one end of the gas bypass line 231 is connected to the cooling gas inlet line 23, and the other end of the gas bypass line 231 is connected to the exhaust gas inlet line 21, part of the exhaust gas is delivered to the cooling zone 202 of the sorption rotor 20 for temperature reduction through the gas bypass line 231.
In addition, the next step is to perform desorption in the desorption zone of step S120: the hot gas is delivered to the desorption region 203 of the adsorption rotor 20 for desorption through the hot gas delivery line 24 connected to the other end of the cold side line 301 of the heat exchanger 30, and the desorption concentrated gas is delivered to at least one air inlet line 12 of the regenerative incinerator 10 through the other end of the desorption concentrated gas line 26. After the step S120 is completed, the next step S130 is performed.
In the step S120, the desorption concentrated gas pipeline 26 is provided with a fan 261 (as shown in fig. 4 and fig. 6) to pump the desorption concentrated gas in the desorption concentrated gas pipeline 26. In addition, a proportional damper (as shown in fig. 3 to fig. 6) is disposed 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 that a communication pipeline 27 is disposed between the cooling gas delivery pipeline 24 and the hot gas delivery pipeline 25, the communication pipeline 27 is disposed with a communication control valve 271, the hot gas delivery pipeline 25 is disposed with a hot gas control valve 251, and the proportional damper is formed by the communication control valve 271 and the hot gas control valve 251, the second implementation design is that a communication pipeline 27 is disposed between the cooling gas delivery pipeline 24 and the hot gas delivery pipeline 25, the communication pipeline 27 is disposed with a communication control valve 271, the cooling gas delivery pipeline 24 is disposed with a cooling control valve 241, and the proportional damper is formed by the communication control valve 271 and the cooling control valve 241, therefore, the air flow can be controlled by adjusting the air flow rate through the designed proportional damper of the communication control valve 271 and the hot air control valve 251 or through the designed proportional damper of the communication control valve 271 and the cooling control valve 241, so that the temperature in the hot air delivery pipeline 25 can be kept at a certain high temperature for the desorption zone 203 of the adsorption rotor 20.
Further, the next step proceeds to step S130 of heat storage gas delivery: the gas in the heating chamber 11 of the regenerative incinerator 10 is transferred to one end of the hot side pipe 302 of the heat exchanger 30 through the regenerative gas recovery pipe 32 connected to the hot gas outlet 111, and then transferred through the hot gas recovery pipe 31 connected to the other end of the hot side pipe 302 of the heat exchanger 30. After the step S130 is completed, the next step S140 is performed.
In the above step S130, the hot gas recycling pipeline 31 has two connecting paths, the first path is that the other end of the hot gas recycling pipeline 31 is connected to the desorption concentrated gas pipeline 26 (as shown in fig. 2 to fig. 4), so that the gas that is transported to the hot side pipeline 302 of the heat exchanger 30 by the heat storage gas recycling pipeline 32 for heat recycling is transported to the desorption concentrated gas pipeline 26 by the hot gas recycling pipeline 31, and then transported to the regenerative incinerator 10 for repeated combustion by the desorption concentrated gas pipeline 26, thereby achieving recycling efficiency.
The second path is when at least three regenerative beds 101 are provided in the regenerative thermal oxidizer 10 or when the regenerative thermal incinerator 10 is a rotary regenerative thermal incinerator (not shown), the regenerative bed 101 of the regenerative thermal oxidizer 10 is provided with a scavenging (purge) line 14 (shown in fig. 5 and 6), and the other end of the scavenging (purge) line 14 is connected to the heating chamber 11, so that when the heat storage bed 101 is not used for the intake air or the exhaust air, the scavenging gas (purge) can be supplied into the heating chamber 11 through the scavenging line 14, and therefore, the other end of the hot gas recovery line 31 is connected to the scavenging ((purge)) line 14, and the gas, which is sent to the hot side line 302 of the heat exchanger 30 through the heat storage gas recovery line 32 and subjected to heat recovery, is sent to the scavenging ((purge)) line 14 through the hot gas recovery line 31 and then sent to the heating chamber 11 through the scavenging ((purge)) line 14.
Further, step S140 next proceeds to exhaust gas recovery conveyance: the gas discharged from the gas outlet line 13 of the regenerative incinerator 10 is transferred to one end of the return hot side line 402 of the return heat exchanger 40 through the return hot gas recovery line 41. After the step S140 is completed, the next step S150 is performed.
In addition, the next step S150 is via a return recovery line: the gas supplied to the return hot-side pipe 402 of the return heat exchanger 40 is supplied to one end of the exhaust gas intake pipe 21 via the return recovery pipe 42 connected to the other end of the return hot-side pipe 402 of the return heat exchanger 40.
Wherein the heat-returning exchanger 40 in the step S150 is connected to a hot-returning gas recycling pipeline 41 and a hot-returning gas recycling pipeline 42, one end of the cold-returning pipeline 401 of the heat-returning exchanger 40 is connected to the other end of the clean gas discharging pipeline 22, and the hot-returning gas is recycledOne end of the pipe 41 is connected to one end of the hot-side return pipe 402 of the return heat exchanger 40 (as shown in fig. 2 to 6), the other end of the hot-gas return pipe 41 is connected to the outlet pipe 13 of the regenerative incinerator 10, one end of the return recovery pipe 42 is connected to the other end of the hot-side return pipe 402 of the return heat exchanger 40, and the other end of the return recovery pipe 42 is connected to the exhaust gas inlet pipe 21. Furthermore, the hot gas return line 41 and the hot gas return line 42 of the heat return exchanger 40 can be provided with a dust removing device 60 (as shown in fig. 6), or a dust removing device 60 is provided on the hot gas return line 42 of the heat return exchanger 40 (as shown in fig. 3 and 5), or a dust removing device 60 is provided on the hot gas return line 41 of the heat return exchanger 40 (as shown in fig. 4), so that the gas passing through the hot gas return line 41 or the gas passing through the hot gas return line 42 can be filtered by the dust removing device 60, wherein the dust removing device 60 is a bag filter, an electric bag filter, an inertial filter, an electrostatic precipitator, a centrifugal precipitator, a filter cartridge pulse precipitator, a pulse bag filter, a pulse filter cartridge precipitator, a pulse filter, a vacuum cleaner, the pulse-jet bag type dust collector, the wet type electric dust collector, the wet type electrostatic dust collector, the water film dust collector, the venturi tube dust collector, the cyclone separator, the flue dust collector, the multilayer dust collector, the negative pressure blowback filter bag dust collector, the low pressure long bag pulse dust collector, the horizontal type electrostatic dust collector, the unpowered dust collector, the charged water mist dust collector, the multi-tube cyclone dust collector, the explosion-proof dust collector, and the backflow recovery pipeline 42 of the backflow heat exchanger 40 is provided with a fan 421 (as shown in fig. 3 to 6) to push the gas in the backflow recovery pipeline 42 into the waste gas inlet pipeline 21. Thus, the gas burned in the regenerative thermal oxidizer 10 is transferred to the hot-side return pipe 402 of the return heat exchanger 40 through the hot-gas return pipe 41 for heat recovery, and then transferred to the dust removing device 60 through the return recovery pipe 42 for dust or silica ((SiO) oxide)2) Etc.) and finally the gas output by the dust-removing device 60 is conveyed to the exhaust gas inlet pipeline21, the combusted gas enters the adsorption zone 201 of the adsorption rotor 20 and is discharged without passing through the chimney 70, so that the discharge amount of the chimney 70 is reduced, and the treatment efficiency of the organic waste gas is improved.
The heat-accumulating backflow high-efficiency organic waste gas treatment system of the second embodiment of the present invention mainly comprises a heat-accumulating incinerator (RTO)10, an adsorbing rotating wheel 20, a heat exchanger 30 and a cooler 50 (as shown in fig. 8 to 12), wherein the heat exchanger 30 has a cold side pipeline 301 and a hot side pipeline 302, the heat exchanger 30 is connected to a hot gas recycling pipeline 31 and a heat-accumulating gas recycling pipeline 32, the cooler 50 is connected to a cooling backflow hot gas recycling pipeline 51 and a cooling backflow recycling pipeline 52, the heat-accumulating incinerator (RTO)10 is provided with a heat-accumulating bed 101, the heat-accumulating bed 101 may be provided with two heat-accumulating beds (as shown in fig. 8 to 10), three heat-accumulating beds (as shown in fig. 11 and 12), four heat-accumulating beds (not shown) or five heat-accumulating beds (not shown), and the heat-accumulating incinerator (RTO)10 is provided with a heating chamber 11, At least one air inlet pipe 12 and at least one air outlet pipe 13, the heating chamber 11 is provided with a hot air outlet 111 (as shown in fig. 8 to 12). Alternatively, the regenerative thermal oxidizer ((RTO))10 may be a rotary regenerative thermal oxidizer ((not shown)).
When the Regenerative Thermal Oxidizer (RTO)10 of the present invention has a heating chamber 11 and at least three regenerative beds 101 (as shown in fig. 11 and 12), the three regenerative beds 101 are respectively provided as a first regenerative bed 1011, a second regenerative bed 1012 and a third regenerative bed 1013, the first regenerative bed 1011, the second regenerative bed 1012 and the third regenerative bed 1013 are all communicated with the heating chamber 11, and the regenerative bed 101 is used for storing and releasing heat to recover the heat energy of the high-temperature exhaust gas for preheating the low-temperature intake air, and the first regenerative bed 1011, the second regenerative bed 1012 or the third regenerative bed 1013 are used by being switched with each other. In addition, the heating chamber 11 of the regenerative thermal oxidizer ((RTO))10 is provided with a burner (see fig. 8 to 12) which introduces fuel gas or fuel liquid for combustion and transfers hot gas during combustion to the heating chamber 11 of the Regenerative Thermal Oxidizer (RTO)10 for use, and the burner is provided with an air line which is provided with a fan for pushing air in the air line into the burner to assist combustion to generate temperature rise.
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 purified 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. 8 to fig. 12), and the other end of the waste gas inlet pipeline 21 is connected to one side a of the adsorption region 201 of the adsorption rotor 20, so that the adsorption region 201 of the adsorption rotor 20 adsorbs the waste gas in the waste gas inlet pipeline 21, and one end of the purified gas discharge pipeline 22 is connected to the other side B 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 purified gas discharge pipeline 22.
In addition, one end of the cooling air inlet pipe 23 is connected to one side a 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. 8 and 9), 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 the cooling air inlet pipe 23 is provided with a gas bypass pipe 231 (as shown in fig. 10), 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 231.
In addition, one end of the cooling gas conveying pipeline 24 is connected to the other side B 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 cold-side pipeline 301 of the heat exchanger 30, so as to convey the cooling gas in the cooling gas conveying pipeline 24 into the heat exchanger 30 for heat exchange (as shown in fig. 8 to 12), the other end of the cold-side pipeline 301 of the heat exchanger 30 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 B of the desorption region 203 of the adsorption rotor 20, one side a 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 heat exchanger 30 is conveyed to the desorption region 203 of the adsorption rotor 20 through the hot gas conveying pipeline 25 for desorption, and the desorption concentrated desorption gas desorbed at high temperature is conveyed and conveyed through the desorption concentrated gas pipeline 26 And the other end of the desorption concentrated gas pipeline 26 is connected to at least one air inlet pipeline 12 of the regenerative incinerator 10, so that the desorption concentrated gas enters the regenerative incinerator 10 for combustion. In addition, the desorption/concentration gas pipeline 26 is provided with a fan 261 (as shown in fig. 10 and 12) for pumping the desorption/concentration gas in the desorption/concentration gas pipeline 26.
In addition, a proportional damper (as shown in fig. 9 to 12) 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, and form the proportional damper 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, and form the proportional damper by the communication control valve 271 and the cooling control valve 241, therefore, the air flow can be controlled by adjusting the design of the communication control valve 271 and the hot air control valve 25 or the design of the communication control valve 271 and the cooling control valve 241, so that the temperature in the hot air delivery pipeline 25 can be kept at a certain high temperature for the desorption region 203 of the adsorption rotor 20.
In addition, the heat exchanger 30 is connected to a hot gas recycling line 31 and a hot gas recycling line 32, wherein one end of the hot gas recycling line 32 is connected to the hot gas outlet 111 of the heating chamber 11 of the regenerative incinerator 10 (as shown in fig. 8 to 12), the other end of the hot gas recycling line 32 is connected to the other end of the hot side line 302 of the heat exchanger 30, and one end of the hot gas recycling line 31 is connected to one end of the hot side line 302 of the heat exchanger 30. Therefore, the desorption concentrated gas is delivered to at least one air inlet pipeline 12 of the regenerative incinerator 10 through the desorption concentrated gas delivery pipeline 26, and the gas combusted by the regenerative incinerator 10 is delivered to the hot side pipeline 302 of the heat exchanger 30 for heat recovery through the regenerative gas recovery pipeline 32 from the hot gas outlet 111 of the heating chamber 11, and is delivered through the hot gas recovery pipeline 31.
The above-mentioned hot gas recycling pipeline 31 has two connecting paths, the first path is that the other end of the hot gas recycling pipeline 31 is connected to the desorption concentrated gas pipeline 26 (as shown in fig. 8 to fig. 10), so that the gas that is transported to the hot side pipeline 302 of the heat exchanger 30 by the heat-storage gas recycling pipeline 32 for heat recycling is transported to the desorption concentrated gas pipeline 26 by the hot gas recycling pipeline 31, and then transported to the heat-storage incinerator 10 for repeated combustion by the desorption concentrated gas pipeline 26, so as to have recycling efficiency.
The second path is when at least three regenerative beds 101 are provided in the regenerative thermal oxidizer 10 or when the regenerative thermal incinerator 10 is a rotary regenerative thermal incinerator (not shown), the regenerative bed 101 of the regenerative thermal oxidizer 10 is provided with a scavenging (purge) line 14 (as shown in fig. 11 and 12), and the other end of the scavenging (purge) line 14 is connected to the heating chamber 11, so that when the heat storage bed 101 is not used for the intake air or the exhaust air, the scavenging gas (purge) can be supplied into the heating chamber 11 through the scavenging line 14, and therefore, the other end of the hot gas recovery line 31 is connected to the scavenging ((purge)) line 14, and the gas, which is sent to the hot side line 302 of the heat exchanger 30 through the heat storage gas recovery line 32 and subjected to heat recovery, is sent to the scavenging ((purge)) line 14 through the hot gas recovery line 31 and then sent to the heating chamber 11 through the scavenging ((purge)) line 14.
In addition, a cooling water pipeline 53 (as shown in fig. 8 to 12) is disposed in the cooler 50, and the cooler 50 is one of a shell-and-tube cooler, a fin-tube cooler, or a plate heat exchanger cooler for cooling the high-temperature hot gas flowing through the cooler 50 in an inlet-outlet manner, the cooler 50 is connected to a cooling return hot gas recovery pipeline 51 and a cooling return recovery pipeline 52, one end of the cooling return hot gas recovery pipeline 51 is connected to one end of the cooler 50, the other end of the cooling return hot gas recovery pipeline 51 is connected to the outlet pipeline 13 of the regenerative incinerator 10, one end of the cooling return recovery pipeline 52 is connected to the other end of the cooler 50, and the other end of the cooling return recovery pipeline 52 is connected to the exhaust gas inlet pipeline 21. Furthermore, the cooling return hot gas recycling line 51 and the cooling return recycling line 52 of the cooler 50 can be provided with a dust removing device 60 at the same time (as shown in fig. 12), or a dust removing device 60 is provided on the cooling return recycling line 52 of the cooler 50 alone (as shown in fig. 9 and 11), or a dust removing device 60 is provided on the cooling return hot gas recycling line 51 of the cooler 50 alone (as shown in fig. 10), so that the gas passing through the cooling return hot gas recycling line 51 or the gas passing through the cooling return recycling line 52 can be filtered by the dust removing device 60, wherein the dust removing device 60 is a bag filter, an electric bag filter, an inertial filter, an electrostatic dust collector, a centrifugal filter, a drum filter, a pulse bag filter, a pulse filter, or a combination filter, The cooling return recovery pipeline 52 of the cooler 50 is provided with a fan 521 (as shown in fig. 8 to 12) to push the gas in the cooling return recovery pipeline 52 into the exhaust gas inlet pipeline 21.
Thus, the gas burned in the regenerative thermal oxidizer 10 is transferred into the cooler 50 through the connected cooling return hot gas recovery line 51 to be heat-exchanged with the cooling water line 53, and is transferred into the dust removing device 60 through the cooling return recovery line 52 to be subjected to dust or silica ((SiO) oxide)2) And finally, the gas output by the dust removal device 60 is conveyed into the waste gas inlet pipeline 21, so that the combusted gas enters the adsorption region 201 of the adsorption rotating wheel 20 for cyclic utilization, and is not discharged through the chimney 70, the discharge amount of the chimney 70 is reduced, and the treatment efficiency of the organic waste gas is improved.
The second embodiment of the present invention relates to a method for treating organic waste gas with high efficiency by heat accumulation reflux, which is mainly used for the organic waste gas treatment system, comprising a heat accumulation type incinerator (RTO)10, an adsorption rotor 20, a heat exchanger 30 and a cooler 50 (as shown in fig. 8 to 12), wherein the heat exchanger 30 is provided with a cold side pipeline 301 and a hot side pipeline 302, the heat exchanger 30 is connected with a hot gas recovery pipeline 31 and a heat accumulation gas recovery pipeline 32, the cooler 50 is connected with a cooling reflux hot gas recovery pipeline 51 and a cooling reflux recovery pipeline 52, the heat accumulation type incinerator (RTO)10 is provided with a heat accumulation bed 101, the heat accumulation bed 101 can be provided with two heat accumulation beds (as shown in fig. 8 to 10), three heat accumulation beds (as shown in fig. 11 and 12), four heat accumulation beds (not shown) or five heat accumulation beds (not shown), and the heat accumulation type incinerator (RTO)10 is provided with a heating chamber 11, and a heating chamber 52, At least one air inlet pipe 12 and at least one air outlet pipe 13, the heating chamber 11 is provided with a hot air outlet 111 (as shown in fig. 8 to 12). Alternatively, the regenerative thermal oxidizer ((RTO))10 may be a rotary regenerative thermal oxidizer ((not shown)).
When the Regenerative Thermal Oxidizer (RTO)10 of the present invention has a heating chamber 11 and at least three regenerative beds 101 (as shown in fig. 11 and 12), the three regenerative beds 101 are respectively provided as a first regenerative bed 1011, a second regenerative bed 1012 and a third regenerative bed 1013, the first regenerative bed 1011, the second regenerative bed 1012 and the third regenerative bed 1013 are all communicated with the heating chamber 11, and the regenerative bed 101 is used for storing and releasing heat to recover the heat energy of the high-temperature exhaust gas for preheating the low-temperature intake air, and the first regenerative bed 1011, the second regenerative bed 1012 or the third regenerative bed 1013 are used by being switched with each other. In addition, the heating chamber 11 of the regenerative thermal oxidizer ((RTO))10 is provided with a burner (as shown in fig. 8 to 12) which introduces fuel gas or fuel liquid for combustion and transfers hot gas during combustion to the heating chamber 11 of the Regenerative Thermal Oxidizer (RTO)10 for use, and the burner is provided with an air line which is provided with a fan for pushing air in the air line into the burner to assist combustion and generate temperature rise.
The main steps of the processing method (as shown in fig. 7) include: step S200 adsorption in adsorption zone: the exhaust gas is fed to one side of the adsorption region 201 of the adsorption rotor 20 through the other end of the exhaust gas inlet line 21 for adsorption, and the adsorbed gas is then delivered through the other end of the purified gas discharge line 22. After the step S200 is completed, the next step S210 is performed.
In the step S200, the other end of the net gas exhaust pipeline 22 is connected to a chimney 70 (as shown in fig. 8 to 12), so that the purified gas exhausted from the net gas exhaust pipeline 22 is delivered to the chimney 70 for exhaust. The clean gas discharge pipe 22 is further provided with a blower 221 for pushing the gas in the clean gas discharge pipe 22 toward the chimney 70.
In addition, the next step S210 cooling zone cooling: the cooling gas is supplied to the cooling zone 202 of the sorption rotor 20 through the other end of the cooling gas inlet conduit 23 for cooling, and the cooling gas passing through the cooling zone 202 is supplied to one end of the cold-side conduit 301 of the heat exchanger 30 through the other end of the cooling gas supply conduit 24. After the step S210 is completed, the next step S220 is performed.
Wherein one end of the cooling gas inlet line 23 is connected to one side a of the cooling zone 202 of the sorption rotor 20 in the above-mentioned step S210, and the cooling gas inlet line 23 has two embodiments, in the first embodiment, the cooling air inlet pipe 23 is used for the entry of external air (as shown in fig. 8 and 9), the external air is fresh air to be delivered to the cooling zone 202 of the sorption rotor 20 for cooling, and in a second embodiment, the cooling air inlet pipe 23 is provided with a gas bypass pipe 231 (as shown in fig. 10), one end of the gas bypass line 231 is connected to the cooling gas inlet line 23, and the other end of the gas bypass line 231 is connected to the exhaust gas inlet line 21, part of the exhaust gas is delivered to the cooling zone 202 of the sorption rotor 20 for temperature reduction by the gas bypass 231.
In addition, the next step is to perform desorption in the desorption zone of step S220: the hot gas is delivered to the desorption region 203 of the adsorption rotor 20 for desorption through the hot gas delivery pipeline 25 connected to the other end of the cold side pipeline 301 of the heat exchanger 30, and the desorption concentrated gas is delivered to at least one air inlet pipeline 12 of the regenerative incinerator 10 through the other end of the desorption concentrated gas pipeline 26. After the step S220 is completed, the next step S230 is performed.
In the step S220, the desorption concentrated gas pipeline 26 is provided with a fan 261 (as shown in fig. 9 to 12) for pumping the desorption concentrated gas in the desorption concentrated gas pipeline 26. In addition, a proportional damper (as shown in fig. 9-12) is disposed 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 that a communication pipeline 27 is disposed between the cooling gas delivery pipeline 24 and the hot gas delivery pipeline 25, the communication pipeline 27 is provided with a communication control valve 271, the hot gas delivery pipeline 25 is provided with a hot gas control valve 251, and the proportional damper is formed by the communication control valve 271 and the hot gas control valve 251, the second implementation design is that a communication pipeline 27 is disposed between the cooling gas delivery pipeline 24 and the hot gas delivery pipeline 25, the communication pipeline 27 is provided with a communication control valve 271, the cooling gas delivery pipeline 24 is provided with a cooling control valve 241, and the proportional damper is formed by the communication control valve 271 and the cooling control valve 241, therefore, the air flow can be controlled by adjusting the air flow rate through the designed proportional damper of the communication control valve 271 and the hot air control valve 251 or through the designed proportional damper of the communication control valve 271 and the cooling control valve 241, so that the temperature in the hot air delivery pipeline 25 can be kept at a certain high temperature for the desorption zone 203 of the adsorption rotor 20.
Further, next step S230 is the heat storage gas delivery: the gas in the heating chamber 11 of the regenerative incinerator 10 is transferred to one end of the hot side pipe 302 of the heat exchanger 30 through the regenerative gas recovery pipe 32 connected to the hot gas outlet 111, and then transferred through the hot gas recovery pipe 31 connected to the other end of the hot side pipe 302 of the heat exchanger 30. After the step S230 is completed, the next step S240 is performed.
In the above step S230, the hot gas recycling pipeline 31 has two connecting paths, the first path is that the other end of the hot gas recycling pipeline 31 is connected to the desorption concentrated gas pipeline 26 (as shown in fig. 8 to fig. 10), so that the gas that is transported to the hot side pipeline 302 of the heat exchanger 30 by the heat storage gas recycling pipeline 32 for heat recycling is transported to the desorption concentrated gas pipeline 26 by the hot gas recycling pipeline 31, and then transported to the heat storage type incinerator 10 for repeated combustion by the desorption concentrated gas pipeline 26, thereby achieving recycling efficiency.
And the second path is that when at least three heat storage beds 101 are provided in the heat storage type incinerator 10 or the heat storage type incinerator 10 is a rotary type heat storage type incinerator (not shown), the heat storage bed 101 of the heat storage type incinerator 10 is provided with a scavenging (purge) pipeline 14 (as shown in fig. 11 and 12), and the other end of the scavenging (purge) pipeline 14 is connected to the heating chamber 11, so that when the heat storage bed 101 is not used for air intake or air exhaust, the scavenging (purge) pipeline 14 can be used for conveying the scavenging gas into the heating chamber 11, therefore, the other end of the hot gas recovery pipeline 31 is connected to the scavenging (purge) pipeline 14, the gas which is conveyed into the hot side pipeline 302 of the heat exchanger 30 by the heat storage gas recovery pipeline 32 for heat recovery is conveyed into the scavenging (purge) pipeline 14 by the hot gas recovery pipeline 31, and then, the exhaust gas is supplied into the heating chamber 11 through the scavenging (purge) pipe 14.
Further, the next step is a step S240 of exhaust gas recovery and transport: the gas discharged from the gas outlet line 13 of the regenerative incinerator 10 is delivered to one end of the cooler 50 through the cooled returned hot gas recovery line 51. After the step S240 is completed, the next step S250 is performed.
In addition, the next step proceeds to step S250 through a cooling return recovery line: the gas supplied to the cooler 50 is supplied to one end of the exhaust gas intake line 21 via a cooling return recovery line 52 connected to the other end of the cooler 50.
In the step S250, the cooler 50 is provided with a cooling water pipeline 53 (as shown in fig. 8 to 12) therein, the cooler 50 cools the high-temperature hot gas flowing through the cooler 50 in an inlet-outlet manner, the cooler 50 is any one of a shell-and-tube cooler, a fin-tube cooler or a plate heat exchanger cooler, the cooling return hot gas recycling pipeline 51 and the cooling return recycling pipeline 52 of the cooler 50 can be provided with a dust removing device 60 at the same time (as shown in fig. 12), or the cooling return recycling pipeline 52 of the cooler 50 is provided with a dust removing device 60 alone (as shown in fig. 9 and 11), or the cooling return hot gas recycling pipeline 51 of the cooler 50 is provided with a dust removing device 60 alone (as shown in fig. 10), so that the gas passing through the cooling return hot gas recycling pipeline 51 or the gas passing through the cooling return recycling pipeline 52 can pass through the dust removing device 60 Filtering, wherein the dust-removing equipment 60 is 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 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 electric dust collector, a wet 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 reverse blowing bag-type dust collector, a low pressure long bag pulse dust collector, a horizontal electrostatic dust collector, a non-power dust collector, a charged water mist dust collector, a multi-tube cyclone dust collector and an explosion-proof dust collector, and the cooling return recovery pipeline 52 of the cooler 50 is provided with a fan 521 (as shown in the figure)8-12) to push the gas in the cooling return recovery line 52 towards the exhaust gas inlet line 21. Thus, the gas burned in the regenerative thermal oxidizer 10 is transferred to the cooler 50 through the connected cooling return hot gas recovery line 51 to be heat-recovered with the cooling water line 53, and is transferred to the dust removing device 60 through the cooling return recovery line 52 to be dust or silica ((SiO) oxide)2) And finally, the gas output by the dust removal device 60 is conveyed into the waste gas inlet pipeline 21, so that the combusted gas enters the adsorption region 201 of the adsorption rotating wheel 20 for cyclic utilization, and is not discharged through the chimney 70, the discharge amount of the chimney 70 is reduced, and the treatment efficiency of the organic waste gas is improved.
The above-mentioned embodiments are intended to illustrate the objects, technical solutions and advantages of the present invention in further detail, and it should be understood that the above-mentioned embodiments are only exemplary embodiments of the present invention and are not intended to limit the present invention, and any modifications, equivalents, improvements and the like made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (46)
1. A heat accumulation backflow high-efficiency organic waste gas treatment system is characterized by comprising:
the heat accumulating type incinerator is provided with a heating chamber, at least one air inlet pipeline and at least one air outlet pipeline, and the heating chamber is provided with a hot air outlet;
an adsorption runner, which is provided with an adsorption area, a cooling area and a desorption area, and is connected with a waste gas inlet pipeline, a purified 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 purified 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, one end of the desorption concentrated gas pipeline is connected with one side of the desorption area of the adsorption rotating wheel, the other end of the desorption concentrated gas pipeline is connected with at least one air inlet pipeline of the regenerative incinerator; and
the heat exchanger is provided with a cold side pipeline and a hot side pipeline, the heat exchanger is connected with a hot gas recovery pipeline and a heat accumulation gas recovery pipeline, one end of the cold side pipeline is connected with the other end of the cooling gas conveying pipeline, the other end of the cold side pipeline is connected with the other end of the hot gas conveying pipeline, one end of the heat accumulation gas recovery pipeline is connected with a hot gas outlet of a heating chamber of the heat accumulation type incinerator, the other end of the heat accumulation gas recovery pipeline is connected with the other end of the hot side pipeline, and one end of the hot gas recovery pipeline is connected with one end of the hot side pipeline; and
a reflux heat exchanger, this reflux heat exchanger is equipped with backward flow cold side pipeline and backward flow hot side pipeline, this reflux heat exchanger is connected with a backward flow steam recovery pipeline and a backward flow recovery pipeline, the one end of this backward flow cold side pipeline is connected with the other end of this net gas emission pipeline, the one end of this backward flow steam recovery pipeline is connected with the one end of this backward flow hot side pipeline, the other end of this backward flow steam recovery pipeline is connected with the play gas pipeline of this heat accumulation formula incinerator, the one end of this backward flow recovery pipeline is connected with the other end of this backward flow hot side pipeline, the other end and this waste gas admission pipe connection of this backward flow recovery pipeline.
2. A heat accumulation backflow high-efficiency organic waste gas treatment system is characterized by comprising:
the heat accumulating type incinerator is provided with a heating chamber, at least one air inlet pipeline and at least one air outlet pipeline, and the heating chamber is provided with a hot air outlet;
an adsorption runner, which is provided with an adsorption area, a cooling area and a desorption area, and is connected with a waste gas inlet pipeline, a purified 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 purified 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, one end of the desorption concentrated gas pipeline is connected with one side of the desorption area of the adsorption rotating wheel, the other end of the desorption concentrated gas pipeline is connected with at least one air inlet pipeline of the regenerative incinerator; and
the heat exchanger is provided with a cold side pipeline and a hot side pipeline, the heat exchanger is connected with a hot gas recovery pipeline and a heat accumulation gas recovery pipeline, one end of the cold side pipeline is connected with the other end of the cooling gas conveying pipeline, the other end of the cold side pipeline is connected with the other end of the hot gas conveying pipeline, one end of the heat accumulation gas recovery pipeline is connected with a hot gas outlet of a heating chamber of the heat accumulation type incinerator, the other end of the heat accumulation gas recovery pipeline is connected with the other end of the hot side pipeline, and one end of the hot gas recovery pipeline is connected with one end of the hot side pipeline; and
the cooler is connected with a cooling reflux hot gas recovery pipeline and a cooling reflux hot gas recovery pipeline, one end of the cooling reflux hot gas recovery pipeline is connected with one end of the cooler, the other end of the cooling reflux hot gas recovery pipeline is connected with the air outlet pipeline of the regenerative thermal incinerator, one end of the cooling reflux recovery pipeline is connected with the other end of the cooler, and the other end of the cooling reflux recovery pipeline is connected with the waste gas inlet pipeline.
3. The regenerative-reflux high-efficiency organic waste gas treatment system according to claim 1, wherein the reflux heat exchanger is further connected to a chimney, the chimney is provided with a chimney discharge pipeline, one end of the chimney discharge pipeline is connected to the chimney, and the other end of the chimney discharge pipeline is connected to the other end of the cold-side pipeline of the reflux heat exchanger.
4. The regenerative flow high efficiency organic waste gas treatment system as claimed in claim 3 wherein the stack exhaust line is further provided with a fan.
5. The regenerative flow high efficiency organic waste gas treatment system according to claim 3, wherein the chimney exhaust line is further connected to a net gas bypass line, one end of the net gas bypass line is connected to the net gas exhaust line, and the other end of the net gas bypass line is connected to the chimney exhaust line.
6. The regenerative flow high efficiency organic waste gas treatment system as claimed in claim 5, wherein the net gas bypass line is further provided with a net gas bypass control valve.
7. The regenerative reflux high efficiency organic waste gas treatment system as set forth in claim 2 wherein the other end of the net gas exhaust line is further connected to a chimney.
8. The regenerative flow high efficiency organic waste gas treatment system according to claim 1 or 2, wherein a communication line is further provided between the cooling gas supply line and the hot gas supply line, the communication line is provided with a communication control valve, the hot gas supply line is provided with a hot gas control valve, and the proportional damper is formed by the communication control valve and the hot gas control valve.
9. The regenerative flow high efficiency organic waste gas treatment system according to claim 1 or 2, wherein a communication line is further provided between the cooling gas delivery line and the hot gas delivery line, the communication line is provided with a communication control valve, the cooling gas delivery line is provided with a cooling control valve, and a proportional damper is formed by the communication control valve and the cooling control valve.
10. The regenerative flow high efficiency organic waste gas treatment system according to claim 1 or 2, wherein the cooling gas inlet pipe further supplies an external gas to the cooling zone of the sorption rotor, and the external gas is fresh air.
11. The regenerative-reflux high-efficiency organic waste gas treatment system as claimed in 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 to the cooling gas inlet pipe, and the other end of the gas bypass pipe is connected to the waste gas inlet pipe.
12. The regenerative reflux high efficiency organic waste gas treatment system as set forth in claim 1 or 2 wherein the clean gas discharge line is further provided with a blower.
13. The regenerative reflux high efficiency organic waste gas treatment system as set forth in claim 1 or 2 wherein the desorption concentrate gas line is further provided with a fan.
14. The heat-accumulating backflow high-efficiency organic waste gas treatment system according to claim 1, wherein the backflow hot gas recovery pipeline of the backflow heat exchanger is further provided with a dust removal device, and the dust removal device is further any one of a bag filter, an electric bag compound dust remover, an inertial dust remover, an electrostatic dust remover, a centrifugal dust remover, a filter cartridge type pulse dust remover, a pulse bag dust remover, a pulse filter element dust remover, a pulse blowing bag dust remover, a wet electric dust remover, a wet electrostatic dust remover, a water film dust remover, a venturi tube dust remover, a cyclone separator, a flue dust remover, a multi-layer dust remover, a negative pressure reverse blowing filter bag dust remover, a low pressure long bag pulse dust remover, a horizontal electrostatic dust remover, a non-power dust remover, a charged water mist dust remover, a multi-tube dust remover, or an explosion-proof dust remover.
15. The heat-accumulating backflow high-efficiency organic waste gas treatment system according to claim 1, wherein the backflow recovery pipeline of the backflow heat exchanger is further provided with a dust removal device, and the dust removal device is further any one of a bag filter, an electric bag compound dust remover, an inertial dust remover, an electrostatic dust remover, a centrifugal dust remover, a cartridge type pulse dust remover, a pulse bag dust remover, a pulse filter element dust remover, a pulse blowing bag dust remover, a wet electric dust remover, a wet electrostatic dust remover, a water film dust remover, a venturi tube dust remover, a cyclone separator, a flue dust remover, a multi-layer dust remover, a negative pressure reverse blowing filter bag dust remover, a low pressure long bag pulse dust remover, a horizontal electrostatic dust remover, a non-power dust remover, a charged water mist dust remover, a cyclone dust remover or an explosion-proof dust remover.
16. The regenerative-reflux high efficiency organic waste gas treatment system as set forth in claim 1 wherein the reflux recovery line of the reflux heat exchanger is further provided with a blower.
17. The regenerative thermal reflux efficient organic waste gas treatment system as set forth in claim 1 or 2, wherein when the regenerative thermal oxidizer is further a rotary regenerative thermal oxidizer or when at least three regenerative beds or more are further provided in the regenerative thermal oxidizer, the regenerative thermal oxidizer is provided with a scavenging (purge) line, and the other end of the scavenging (purge) line is connected to the heating chamber.
18. The regenerative-reflux high-efficiency organic waste gas treatment system as claimed in claim 17, wherein the scavenging (purge) line is further connected to the other end of the hot gas recovery line.
19. The regenerative reflux high efficiency organic waste gas treatment system as set forth in claim 1 or 2, wherein the other end of the hot gas recovery line is further connected to the desorption concentrate gas line.
20. The regenerative flow high efficiency organic waste gas treatment system according to claim 2, wherein the cooler is further any one of a shell and tube cooler, a fin tube cooler, or a plate heat exchanger cooler.
21. The heat-accumulative reflux high-efficiency organic waste gas treating system according to claim 2, wherein the cooling reflux hot gas recycling line of the cooler is further provided with a dust-removing device, and the dust-removing device is further any one of a bag filter, an electric bag compound dust collector, an inertial dust collector, an electrostatic dust collector, a centrifugal dust collector, a cartridge type pulse dust collector, a pulse bag filter, a pulse filter cartridge dust collector, a pulse-jet bag filter, a wet dust collector, a wet electric dust collector, a wet 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 reverse-blowing filter bag dust collector, a low pressure long bag pulse dust collector, a horizontal electrostatic dust collector, a non-dynamic dust collector, a charged water mist dust collector, a multi-tube dust collector or an explosion-proof dust collector.
22. The heat-accumulating backflow high-efficiency organic waste gas treatment system according to claim 2, wherein the cooling backflow recovery pipeline of the cooler is further provided with a dust removal device, and the dust removal device is further any one of a bag filter, an electric bag compound dust remover, an inertial dust remover, an electrostatic dust remover, a centrifugal dust remover, a filter cartridge type pulse dust remover, a pulse bag dust remover, a pulse filter element dust remover, a pulse blowing bag dust remover, a wet electric dust remover, a wet electrostatic dust remover, a water film dust remover, a venturi tube dust remover, a cyclone separator, a flue dust remover, a multi-layer dust remover, a negative pressure reverse blowing filter bag dust remover, a low pressure long bag pulse dust remover, a horizontal electrostatic dust remover, a non-power dust remover, a charged water mist dust remover, a multi-tube dust remover or an explosion-proof dust remover.
23. The regenerative-reflux high-efficiency organic waste gas treatment system as set forth in claim 2, wherein the cooling-reflux recovery line of the cooler is further provided with a fan.
24. A heat-accumulating reflux high-efficiency organic waste gas treating method is mainly used for the organic waste gas treating system and is characterized by comprising a heat-accumulating incinerator, an adsorption rotating wheel, a heat exchanger and a reflux heat exchanger, wherein the heat-accumulating incinerator is provided with a heating chamber, at least one air inlet pipeline and at least one air outlet pipeline, the heating chamber is provided with a hot gas outlet, the adsorption rotating wheel is provided with an adsorption area, a desorption area and a cooling area, the adsorption rotating wheel is connected with a waste gas inlet pipeline, a purified 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 heat exchanger is provided with a cold side pipeline and a hot side pipeline, the heat exchanger is connected with a hot gas recovery pipeline and a heat-accumulating gas recovery pipeline, the reflux heat exchanger is provided with a reflux cold side pipeline and a hot side, the reflux heat exchanger is connected with a reflux hot gas recovery pipeline and a reflux recovery pipeline, and the treatment method mainly comprises the following steps:
adsorption in an adsorption zone: waste gas is sent to one side of an adsorption area of the adsorption rotating wheel for adsorption through the other end of the waste gas inlet pipeline, and the adsorbed gas is conveyed to one end of a backflow cold side pipeline of the backflow heat exchanger through the other end of the purified gas discharge pipeline;
cooling in a cooling area: conveying cooling gas to a cooling area of the adsorption rotating wheel for cooling through the other end of the cooling gas inlet pipeline, and conveying the cooling gas passing through the cooling area to one end of a cold side pipeline of the heat exchanger through the other end of the cooling gas conveying pipeline;
desorption in a desorption area: the hot gas is conveyed to a desorption area of the adsorption rotating wheel for desorption through a hot gas conveying pipeline connected with the other end of the cold side pipeline of the heat exchanger, and then the desorption concentrated gas is conveyed to at least one air inlet pipeline of the regenerative incinerator through the other end of the desorption concentrated gas pipeline;
and (3) conveying heat storage gas: conveying the gas in the heating chamber of the regenerative incinerator to one end of a hot side pipeline of the heat exchanger through a regenerative gas recovery pipeline connected with the hot gas outlet, and then conveying the gas through a hot gas recovery pipeline connected with the other end of the hot side pipeline of the heat exchanger;
and (3) recovering and conveying the exhaust gas: gas discharged by the gas outlet pipeline of the regenerative incinerator is conveyed to one end of a backflow hot side pipeline of the backflow heat exchanger through the backflow hot gas recovery pipeline; and
through a return recovery pipeline: and conveying the gas conveyed to the return hot side pipeline of the return heat exchanger to one end of the waste gas inlet pipeline through a return recovery pipeline connected with the other end of the return hot side pipeline of the return heat exchanger.
25. A heat accumulation backflow high-efficiency organic waste gas treatment method is mainly used for an organic waste gas treatment system and is characterized by comprising a heat accumulation type incinerator, an adsorption rotating wheel, a heat exchanger and a cooler, wherein the heat accumulation type incinerator is provided with a heating chamber, at least one air inlet pipeline and at least one air outlet pipeline, the heating chamber is provided with a hot gas outlet, the adsorption rotating wheel is provided with an adsorption area, a desorption area and a cooling area, the adsorption rotating wheel is connected with a waste gas inlet pipeline, a purified 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 heat exchanger is provided with a cold side pipeline and a hot side pipeline, the heat exchanger is connected with a hot gas recovery pipeline and a heat accumulation gas recovery pipeline, the cooler is connected with a cooling backflow hot gas recovery pipeline and a cooling backflow recovery pipeline, the processing method mainly comprises the following steps:
adsorption in an adsorption zone: waste gas is sent to one side of an adsorption area of the adsorption rotating wheel for adsorption through the other end of the waste gas inlet pipeline, and the adsorbed gas is conveyed through the other end of the purified gas discharge pipeline;
cooling in a cooling area: conveying cooling gas to a cooling area of the adsorption rotating wheel for cooling through the other end of the cooling gas inlet pipeline, and conveying the cooling gas passing through the cooling area to one end of a cold side pipeline of the heat exchanger through the other end of the cooling gas conveying pipeline;
desorption in a desorption area: the hot gas is conveyed to a desorption area of the adsorption rotating wheel for desorption through a hot gas conveying pipeline connected with the other end of the cold side pipeline of the heat exchanger, and then the desorption concentrated gas is conveyed to at least one air inlet pipeline of the regenerative incinerator through the other end of the desorption concentrated gas pipeline;
and (3) conveying heat storage gas: conveying the gas in the heating chamber of the regenerative incinerator to one end of a hot side pipeline of the heat exchanger through a regenerative gas recovery pipeline connected with the hot gas outlet, and then conveying the gas through a hot gas recovery pipeline connected with the other end of the hot side pipeline of the heat exchanger;
and (3) recovering and conveying the exhaust gas: conveying the gas discharged from the gas outlet pipeline of the regenerative incinerator to one end of the cooler through the cooling reflux hot gas recovery pipeline; and
passing through a cooling reflux recovery pipeline: the gas delivered to the cooler is delivered to one end of the exhaust gas intake line via a cooling return recovery line connected to the other end of the cooler.
26. The method of claim 24, wherein the heat-accumulating reflux high-efficiency organic waste gas treatment method is characterized in that the reflux heat exchanger is further connected with a chimney, 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 cold-side pipeline of the reflux heat exchanger.
27. The method of claim 26, wherein the chimney exhaust line is further provided with a fan.
28. The method of claim 26, wherein the chimney exhaust line is further connected to a purge bypass line, one end of the purge bypass line is connected to the purge exhaust line, and the other end of the purge bypass line is connected to the chimney exhaust line.
29. The method of claim 28, wherein the net gas bypass line further comprises a net gas bypass control valve.
30. The method of claim 25, wherein the other end of the purge gas exhaust line is further connected to a chimney.
31. The method according to claim 24 or 25, wherein a communication line is further provided 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.
32. The method according to claim 24 or 25, wherein a communication line is further provided between the cooling gas delivery line and the hot gas delivery line, the communication line is provided with a communication control valve, the cooling gas delivery line is provided with a cooling control valve, and a proportional damper is formed by the communication control valve and the cooling control valve.
33. The method of claim 24 or 25, 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.
34. The regenerative-recirculation high-efficiency organic waste gas treatment method as claimed in claim 24 or 25, wherein the cooling gas inlet pipe is further provided with a gas bypass pipe, one end of the gas bypass pipe is connected to the cooling gas inlet pipe, and the other end of the gas bypass pipe is connected to the waste gas inlet pipe.
35. The method according to claim 24 or 25, wherein the net gas discharge pipeline is further provided with a fan.
36. The method according to claim 24 or 25, wherein the desorption/concentration gas pipeline is further provided with a fan.
37. The method according to claim 24, wherein the backflow hot gas recycling line of the backflow heat exchanger is further provided with a dust removing device, and the dust removing device 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 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 reverse blowing filter bag dust collector, a low pressure long bag type pulse dust collector, a horizontal type electrostatic dust collector, a non-power dust collector, a charged water mist dust collector, a multi-tube dust collector, or an explosion-proof dust collector.
38. The method according to claim 24, wherein the recycling line of the heat-storage recycling heat exchanger is further provided with a dust-removing device, and the dust-removing device is further any one of a bag filter, an electric bag filter, an inertial dust collector, an electrostatic dust collector, a centrifugal dust collector, a cartridge-type pulse dust collector, a pulse bag filter, a pulse filter cartridge dust collector, a pulse-jet bag filter, a wet dust collector, a wet electric dust collector, a wet 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 reverse-blowing filter bag dust collector, a low pressure long bag pulse dust collector, a horizontal electrostatic dust collector, a non-powered dust collector, a charged water mist dust collector, a cyclone dust collector, or an explosion-proof dust collector.
39. The method of claim 24, wherein the return recovery line of the heat recovery heat exchanger is further provided with a blower.
40. The regenerative thermal reflux efficient organic waste gas treatment method as set forth in claim 24 or 25, wherein when the regenerative thermal oxidizer is further a rotary regenerative thermal oxidizer or when at least three regenerative beds or more are further provided in the regenerative thermal oxidizer, the regenerative thermal oxidizer is provided with a scavenging (purge) line, and the other end of the scavenging (purge) line is connected to the heating chamber.
41. The method of claim 40, wherein the scavenging (purge) line is further connected to the other end of the hot gas recycling line.
42. The regenerative thermal refluxing high efficiency organic waste gas treating method as claimed in claim 24 or 25, wherein the other end of the hot gas recycling line is further connected to the desorption concentrated gas line.
43. The method of claim 25, wherein the cooler is further any one of a shell-and-tube cooler, a fin-tube cooler, or a plate heat exchanger cooler.
44. The method according to claim 25, wherein the cooling reflux hot gas recovery pipeline of the cooler is further provided with a dust removal device, and the dust removal device is further one of a bag filter, an electric bag filter, an inertial dust collector, an electrostatic dust collector, a centrifugal dust collector, a cartridge pulse dust collector, a pulse bag filter, a pulse filter element dust collector, a pulse blowing bag filter, a wet dust collector, a wet 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 blowback filter bag dust collector, a low pressure long bag pulse dust collector, a horizontal 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.
45. The method according to claim 25, wherein the cooling reflux recovery line of the cooler is further provided with a dust removing device, and the dust removing device is further any one of a bag filter, an electric bag filter, an inertial dust collector, an electrostatic dust collector, a centrifugal dust collector, a cartridge type pulse dust collector, a pulse bag filter, a pulse filter element dust collector, a pulse blowing bag filter, a wet dust collector, a wet electric dust collector, a wet 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 reverse blowing filter bag dust collector, a low pressure long bag pulse dust collector, a horizontal electrostatic dust collector, a non-power dust collector, a charged water mist dust collector, a multi-tube dust collector, or an explosion-proof dust collector.
46. The method according to claim 25, wherein the cooling return recovery line of the cooler is further provided with a blower.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| TW108128018 | 2019-08-07 | ||
| TW108128018A TWI722522B (en) | 2019-08-07 | 2019-08-07 | Heat storage reflux high-efficiency organic waste gas treatment system and method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN112344352A true CN112344352A (en) | 2021-02-09 |
Family
ID=74367852
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910929242.1A Pending CN112344352A (en) | 2019-08-07 | 2019-09-27 | Heat accumulation backflow high-efficiency organic waste gas treatment system and method |
Country Status (2)
| Country | Link |
|---|---|
| CN (1) | CN112344352A (en) |
| TW (1) | TWI722522B (en) |
Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2009018303A (en) * | 2008-06-09 | 2009-01-29 | Sintokogio Ltd | Exhaust gas treatment system |
| TW201617125A (en) * | 2014-11-06 | 2016-05-16 | Jg Environmental Tech Co Ltd | Organic exhaust adsorption concentration purification system and method thereof |
| CN205481039U (en) * | 2016-02-04 | 2016-08-17 | 杰智环境科技股份有限公司 | Use concentrated purification treatment system of waste gas of incinerator heat recovery |
| CN205517129U (en) * | 2016-02-01 | 2016-08-31 | 杰智环境科技股份有限公司 | Use concentrated purification treatment system of waste gas of incinerator heat recovery |
| CN206430171U (en) * | 2016-12-27 | 2017-08-22 | 嘉园环保有限公司 | A kind of thermal accumulating incinerator with residual heat recovery |
| TWM576072U (en) * | 2018-11-09 | 2019-04-01 | 華懋科技股份有限公司 | Energy-saving high concentration double processing system |
| TWM579063U (en) * | 2019-01-21 | 2019-06-11 | 華懋科技股份有限公司 | Thermal oxidation backflow high-efficiency organic waste gas processing system |
| TWM580457U (en) * | 2019-02-01 | 2019-07-11 | 華懋科技股份有限公司 | Thermally oxidized reflow, heat recovery, and high-efficiency organic exhaust treatment system |
| CN211384444U (en) * | 2019-08-07 | 2020-09-01 | 华懋科技股份有限公司 | Heat accumulation backward flow high efficiency organic waste gas processing system |
Family Cites Families (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP3095531B2 (en) * | 1992-06-02 | 2000-10-03 | 株式会社タクマ | Exhaust heat recovery unit for thermal storage deodorizer |
| JP5744488B2 (en) * | 2010-11-29 | 2015-07-08 | 本田技研工業株式会社 | Exhaust gas treatment equipment |
| CN104470620B (en) * | 2012-08-29 | 2017-02-22 | 新东工业株式会社 | Exhaust gas purification facility and method for controlling operation of same |
| TWM548246U (en) * | 2017-02-03 | 2017-09-01 | Jg Environmental Technology Co Ltd | Rolling-wheel ultra-efficient purification system |
| TWM549655U (en) * | 2017-05-12 | 2017-10-01 | 華懋科技股份有限公司 | Volatile organic exhaust gas treatment system with dual treatment structures |
| CN208295930U (en) * | 2018-04-10 | 2018-12-28 | 江苏大信环境科技有限公司 | A kind of novel nitrogen-containing organic exhaust gas heat-storage type incineration treatment device |
| CN108939821B (en) * | 2018-10-15 | 2024-03-26 | 江苏永春环境工程有限公司 | Zeolite rotary wheel adsorption concentration device |
-
2019
- 2019-08-07 TW TW108128018A patent/TWI722522B/en active
- 2019-09-27 CN CN201910929242.1A patent/CN112344352A/en active Pending
Patent Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2009018303A (en) * | 2008-06-09 | 2009-01-29 | Sintokogio Ltd | Exhaust gas treatment system |
| TW201617125A (en) * | 2014-11-06 | 2016-05-16 | Jg Environmental Tech Co Ltd | Organic exhaust adsorption concentration purification system and method thereof |
| CN205517129U (en) * | 2016-02-01 | 2016-08-31 | 杰智环境科技股份有限公司 | Use concentrated purification treatment system of waste gas of incinerator heat recovery |
| CN205481039U (en) * | 2016-02-04 | 2016-08-17 | 杰智环境科技股份有限公司 | Use concentrated purification treatment system of waste gas of incinerator heat recovery |
| CN206430171U (en) * | 2016-12-27 | 2017-08-22 | 嘉园环保有限公司 | A kind of thermal accumulating incinerator with residual heat recovery |
| TWM576072U (en) * | 2018-11-09 | 2019-04-01 | 華懋科技股份有限公司 | Energy-saving high concentration double processing system |
| TWM579063U (en) * | 2019-01-21 | 2019-06-11 | 華懋科技股份有限公司 | Thermal oxidation backflow high-efficiency organic waste gas processing system |
| TWM580457U (en) * | 2019-02-01 | 2019-07-11 | 華懋科技股份有限公司 | Thermally oxidized reflow, heat recovery, and high-efficiency organic exhaust treatment system |
| CN211384444U (en) * | 2019-08-07 | 2020-09-01 | 华懋科技股份有限公司 | Heat accumulation backward flow high efficiency organic waste gas processing system |
Also Published As
| Publication number | Publication date |
|---|---|
| TW202107016A (en) | 2021-02-16 |
| TWI722522B (en) | 2021-03-21 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN210772223U (en) | High-efficiency organic waste gas treatment system for direct-combustion backflow heat recovery | |
| CN211384445U (en) | Organic waste gas concentration heat accumulation combustion backflow cooling system | |
| CN210206363U (en) | Organic waste gas treatment system with high efficiency of backflow heat recovery | |
| TWI741341B (en) | Organic waste gas concentrated heat storage combustion backflow system and method | |
| CN210495806U (en) | High efficiency organic waste gas treatment system with energy recovery | |
| CN210511720U (en) | Direct-fired backflow high-efficiency organic waste gas treatment system | |
| CN211384444U (en) | Heat accumulation backward flow high efficiency organic waste gas processing system | |
| CN211146511U (en) | Organic waste gas concentration heat accumulation combustion reflux system | |
| CN111520731B (en) | Direct-combustion backflow heat recovery organic waste gas treatment system and method | |
| CN211216075U (en) | Catalyst backflow high-efficiency organic waste gas treatment system | |
| CN210410092U (en) | Backflow high-efficiency organic waste gas treatment system | |
| CN112344352A (en) | Heat accumulation backflow high-efficiency organic waste gas treatment system and method | |
| CN111804122A (en) | High-efficiency organic waste gas treatment system and method for reflux heat recovery | |
| CN211384442U (en) | Direct-combustion flow-dividing high-efficiency organic waste gas treatment system | |
| CN206176411U (en) | Energy -saving organic waste gas processing apparatus | |
| CN112337267A (en) | Organic waste gas concentration heat storage combustion backflow cooling system and method thereof | |
| CN111457398A (en) | Direct-combustion backflow high-efficiency organic waste gas treatment system and method | |
| CN112337296B (en) | Catalyst backflow high-efficiency organic waste gas treatment system and method thereof | |
| TWI718521B (en) | Reflux high-efficiency organic waste gas treatment system and method | |
| CN210584335U (en) | Rotating wheel structure of high-efficiency volatile organic waste gas treatment system | |
| CN210495805U (en) | High-efficiency volatile organic waste gas treatment system | |
| CN114060830A (en) | Energy-saving single-runner high-concentration cold-side bypass over-temperature control system and method thereof |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20210209 |
|
| WD01 | Invention patent application deemed withdrawn after publication |