CN114060829A - Energy-saving single-runner cold-side bypass over-temperature control system and method thereof - Google Patents
Energy-saving single-runner cold-side bypass over-temperature control system and method thereof Download PDFInfo
- Publication number
- CN114060829A CN114060829A CN202010958034.7A CN202010958034A CN114060829A CN 114060829 A CN114060829 A CN 114060829A CN 202010958034 A CN202010958034 A CN 202010958034A CN 114060829 A CN114060829 A CN 114060829A
- Authority
- CN
- China
- Prior art keywords
- pipeline
- gas
- cold
- adsorption
- heat exchanger
- 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
- 238000000034 method Methods 0.000 title claims abstract description 25
- 239000007789 gas Substances 0.000 claims abstract description 366
- 238000003795 desorption Methods 0.000 claims abstract description 176
- 238000001179 sorption measurement Methods 0.000 claims abstract description 157
- 239000010815 organic waste Substances 0.000 claims abstract description 19
- 230000001105 regulatory effect Effects 0.000 claims abstract description 11
- 239000000112 cooling gas Substances 0.000 claims description 66
- 238000001816 cooling Methods 0.000 claims description 49
- 238000002485 combustion reaction Methods 0.000 claims description 26
- 238000004891 communication Methods 0.000 claims description 24
- 239000002912 waste gas Substances 0.000 claims description 21
- 230000001276 controlling effect Effects 0.000 claims description 9
- 238000012546 transfer Methods 0.000 claims description 9
- 238000010926 purge Methods 0.000 claims 1
- 239000012855 volatile organic compound Substances 0.000 abstract description 24
- 238000011084 recovery Methods 0.000 abstract description 8
- 230000000694 effects Effects 0.000 description 12
- 238000010586 diagram Methods 0.000 description 5
- 238000003915 air pollution Methods 0.000 description 3
- 238000013461 design Methods 0.000 description 3
- 238000012545 processing Methods 0.000 description 3
- 239000004065 semiconductor Substances 0.000 description 3
- 238000011144 upstream manufacturing Methods 0.000 description 3
- 229910021536 Zeolite Inorganic materials 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
- 239000000463 material Substances 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000010457 zeolite Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000005693 optoelectronics 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/06—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds
-
- 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
-
- 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
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
- F23G5/50—Control or safety arrangements
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G2206/00—Waste heat recuperation
- F23G2206/10—Waste heat recuperation reintroducing the heat in the same process, e.g. for predrying
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G2209/00—Specific waste
- F23G2209/14—Gaseous waste or fumes
Landscapes
- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention relates TO an energy-saving single-runner cold-side bypass over-temperature control system and a method thereof, which are mainly used for an organic waste gas treatment system, and are provided with a direct-fired incinerator (TO), a first heat exchanger, a second heat exchanger, a first cold-side conveying pipeline, an adsorption runner and a chimney, wherein a cold-side proportional air door is additionally arranged between a desorption concentrated gas pipeline and the first cold-side conveying pipeline or on the desorption concentrated gas pipeline, so that when the concentration of Volatile Organic Compounds (VOCs) is increased, the air volume can be regulated and controlled through the cold-side proportional air door, the heat recovery quantity or concentration can be regulated, and the direct-fired incinerator (TO) can be prevented from being over-temperature caused by too high incinerator temperature and even being shut down when the organic waste gas is treated.
Description
Technical Field
The invention relates TO an energy-saving single-runner high-cold side bypass over-temperature control system and a method thereof, which can have the efficiency of adjusting heat recovery amount or concentration when the concentration of Volatile Organic Compounds (VOCs) is high, so that when organic waste gas is treated, a direct-fired incinerator (TO) can be prevented from being over-temperature caused by too high incinerator temperature and even being stopped, and the system is suitable for organic waste gas treatment systems or similar equipment in the semiconductor industry, the photoelectric industry or the chemical industry.
Background
At present, volatile organic gases (VOC) are generated in the manufacturing process of semiconductor industry or photoelectric industry, so that processing equipment for processing the VOC is installed in each factory to prevent the VOC from being directly discharged into the air to cause air pollution. At present, most of the concentrated gas desorbed by the treatment equipment is conveyed to an incinerator for combustion, and the combusted gas is conveyed to a chimney for emission.
However, in recent years, air pollution is very important at home and abroad, so that relevant air quality standards are established on the emission standards of chimneys, and the air pollution is developed according to the international regulation trend and is examined periodically.
Therefore, in view of the above-mentioned drawbacks, the present invention provides an energy-saving single-runner cold-side bypass over-temperature control system and method thereof for improving organic waste gas treatment efficiency, which can be easily operated and assembled by a user and provide convenience to the user.
Disclosure of Invention
The invention mainly aims to provide an energy-saving single-runner cold-side bypass over-temperature control system and a method thereof, which are mainly used for an organic waste gas treatment system, and is provided with a direct-fired incinerator (TO), a first heat exchanger, a second heat exchanger, a first cold-side delivery pipe, an adsorption runner and a chimney, and a cold side proportion air door is additionally arranged between the desorption concentrated gas pipeline and the first cold side conveying pipeline or on the desorption concentrated gas pipeline, therefore, when the concentration of Volatile Organic Compounds (VOCs) becomes high, the air quantity can be regulated and controlled through the cold-side proportional air door, the device has the effect of adjusting the heat recovery quantity or concentration, so that when organic waste gas is treated, the direct-fired incinerator (TO) can be prevented from generating an over-temperature phenomenon due TO too high incinerator temperature and even causing shutdown, and the overall practicability is further improved.
Another objective of the present invention is to provide an energy-saving single-runner cold-side bypass over-temperature control system and method thereof, wherein a cold-side proportional damper is additionally disposed between the concentrated desorption gas pipeline and the first cold-side transport pipeline, when the concentration of Volatile Organic Compounds (VOCs) in the first cold-side transport pipeline increases, the cold-side proportional damper can be used to transport part of the concentrated desorption gas in the concentrated desorption gas pipeline into the first cold-side transport pipeline, so that the concentrated desorption gas in the first cold-side transport pipeline can be mixed with part of the concentrated desorption gas in the concentrated desorption gas pipeline, and the part of the concentrated desorption gas in the concentrated desorption gas pipeline with a lower temperature can lower the temperature of the concentrated desorption gas in the first cold-side transport pipeline with a higher temperature, thereby having the effect of adjusting the heat recovery amount or concentration, the direct-fired incinerator (TO) can be prevented from generating an over-temperature phenomenon caused by too high incinerator temperature and even causing shutdown, and further the whole usability is increased.
Another objective of the present invention is to provide an energy-saving single-runner cold-side bypass over-temperature control system and method thereof, wherein a cold-side proportional damper is additionally disposed on the desorption concentrated gas pipeline, and the other end of the cold-side proportional damper is used for allowing external air to enter, wherein the external air can be fresh air or other gas, so that when the desorption concentrated gas generated in the desorption region of the adsorption runner enters the desorption concentrated gas pipeline and the temperature in the desorption concentrated gas pipeline becomes higher or the concentration becomes higher, the external air input from the other end of the cold-side proportional damper can be used for adjustment, so that the desorption concentrated gas in the desorption concentrated gas pipeline can achieve the effect of reducing the temperature or the concentration, thereby increasing the overall operability.
For a better understanding of the features, nature, and technical content of the present invention, reference should be made to the following detailed description of the invention along 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 schematic diagram of a system in which a first heat exchanger is disposed on the right side of a second heat exchanger according to the present invention.
Fig. 2 is a schematic diagram of a system configuration in which a first heat exchanger is disposed to the left of a second heat exchanger according to the present invention.
FIG. 3 is a schematic diagram of another system configuration in which the first heat exchanger is disposed to the right of the second heat exchanger according to the present invention.
Fig. 4 is a schematic diagram of another system configuration in which the first heat exchanger is disposed to the left of the second heat exchanger according to the present invention.
FIG. 5 is a flow chart of the main steps of the first embodiment of the present invention.
FIG. 6 is a flow chart of the main steps of the second embodiment of the present invention.
FIG. 7 is a flow chart of the main steps of a third embodiment of the present invention.
Fig. 8 is a flow chart of the main steps of the fourth embodiment of the present invention.
Reference numerals:
10: direct-fired incinerators (TO); 101: a furnace end; 102: a hearth; 11: an inlet; 12: an outlet; 20: a first heat exchanger; 21: a first cold-side pipe; 22: a first hot side duct; 23: a first cold-side transfer line; 30: a second heat exchanger; 31. a second cold-side pipe; 32. a second hot side duct; 60: an adsorption rotating wheel; 601: an adsorption zone; 602: a cooling zone; 603: a desorption zone; 61: an exhaust gas inlet line; 611: exhaust gas communication line 6111: the waste gas is communicated with a control valve; 62: a clean gas discharge line; 621: a clean gas communication pipeline; 6211: a control valve is communicated with the purified gas; 63: a cooling gas inlet line; 64: a cooling gas delivery line; 65: a hot gas delivery line; 66: a concentrated gas desorption pipeline; 661: a fan; 80: a chimney; 901: a cold side proportional damper; 904: a cold side proportional damper; s100: inputting gas to be adsorbed; s200: inputting gas to be adsorbed; s110: the adsorption runner carries out adsorption; s210: the adsorption runner carries out adsorption; s120: inputting cooling gas; s220: inputting cooling gas; s130: conveying hot gas for desorption; s230: conveying hot gas for desorption; s140: conveying the desorbed and concentrated gas; s240: conveying the desorbed and concentrated gas; s150: conveying the burned gas; s250: conveying the burned gas; s160: regulating and controlling a cold side proportional air door; s260: regulating and controlling a cold side proportional air door; s300: inputting gas to be adsorbed; s400: inputting gas to be adsorbed;
s310: the adsorption runner carries out adsorption; s410: the adsorption runner carries out adsorption; s320: inputting cooling gas; s420: inputting cooling gas; s330: conveying hot gas for desorption; s430: conveying hot gas for desorption; s340: conveying the desorbed and concentrated gas; s440: conveying the desorbed and concentrated gas; s350: conveying the burned gas; s450: conveying the burned gas; s360: regulating and controlling a cold side proportional air door; s460: and regulating and controlling a cold-side proportional air door.
Detailed Description
Referring TO fig. 1 TO 8, fig. 1 TO 8 are schematic diagrams of embodiments of the present invention, and the best implementation of the energy-saving single-runner cold-side bypass over-temperature control system and the method thereof of the present invention is applied TO a Volatile Organic Compounds (VOCs) processing system or the like in the semiconductor industry, the optoelectronic industry or the chemical industry, and mainly has an effect of adjusting the heat recovery amount or concentration when the concentration of the VOCs becomes high, so that the organic waste gas can be treated without over-temperature of the direct combustion incinerator (TO) due TO too high incinerator temperature, even causing shutdown.
The energy-saving single-runner cold-side bypass over-temperature control system of the present invention mainly comprises a combination design of a direct-fired incinerator (TO)10, a first heat exchanger 20, a second heat exchanger 30, a first cold-side delivery pipe 23, an adsorption runner 60 and a chimney 80 (as shown in fig. 1 TO 4), wherein the first heat exchanger 20 is provided with a first cold-side pipe 21 and a first hot-side pipe 22, and the second heat exchanger 30 is provided with a second cold-side pipe 31 and a second hot-side pipe 32. The direct-fired incinerator (TO)10 is provided with a burner 101 and a hearth 102, the burner 101 is communicated with the hearth 102, the first heat exchanger 20 and the second heat exchanger 30 are respectively arranged in the hearth 102 of the direct-fired incinerator (TO)10, the direct-fired incinerator (TO)10 is provided with an inlet 11 and an outlet 12 (as shown in fig. 1 TO 4), the inlet 11 is arranged at the burner 101, the merging port 11 is connected with the other end of the first cold-side pipeline 21 of the first heat exchanger 20, the outlet 12 is arranged at the hearth 102, and the outlet 12 is connected TO the chimney 80, so that organic waste gas can enter the burner 101 from the inlet 11 TO be combusted, and combusted gas can pass through the hearth 102 and be discharged TO the chimney 80 from the outlet 12 TO be discharged, thereby having the energy-saving effect.
The first heat exchanger 20 has two embodiments, wherein the first heat exchanger 20 is disposed at the right side of the second heat exchanger 30 (as shown in fig. 1 and 3), so that the burner 101 of the direct combustion incinerator (TO)10 can firstly deliver the burned high-temperature gas TO one side of the second hot-side pipeline 32 of the second heat exchanger 30 for heat exchange, then deliver the burned high-temperature gas TO one side of the first hot-side pipeline 22 of the first heat exchanger 20 for heat exchange from the other side of the second hot-side pipeline 32 of the second heat exchanger 30, finally deliver the burned high-temperature gas TO the outlet 12 of the furnace 102 from the other side of the first hot-side pipeline 22 of the first heat exchanger 20 (as shown in fig. 1 and 2), and deliver the burned high-temperature gas TO the chimney 80 from the outlet 12 of the furnace 102 for emission through the chimney 80.
In the second embodiment, the first heat exchanger 20 is disposed on the left side of the third heat exchanger 40 (as shown in FIGS. 2 and 4),make itThe burner 101 of the direct combustion type incinerator (TO)10 can firstly deliver the incinerated high-temperature gas TO one side of the first hot side pipeline 22 of the first heat exchanger 20 for heat exchange, and then re-deliver the incinerated high-temperature gas TO one side of the second hot side pipeline 32 of the second heat exchanger 30 for heat exchange from the other side of the first hot side pipeline 22 of the first heat exchanger 20, and then re-deliver the incinerated high-temperature gas TO the outlet 12 of the furnace 102 from the other side of the second hot side pipeline 32 of the second heat exchanger 30 (as shown in fig. 3 and 4), and then deliver the incinerated high-temperature gas TO the chimney 80 from the outlet 12 of the furnace 102 for discharge through the chimney 80.
The adsorption rotor 60 of the present invention has an adsorption zone 601, a cooling zone 602 and a desorption zone 603, and the adsorption rotor 60 is connected to a waste gas inlet line 61, a clean gas discharge line 62, a cooling gas inlet line 63, a cooling gas delivery line 64, a hot gas delivery line 65 and a desorption concentrated gas line 66 (as shown in fig. 1 to 4). Wherein the adsorption rotor 60 is a zeolite concentration rotor or a concentration rotor made of other materials.
Wherein one end of the waste gas inlet pipe 61 is connected to one side of the adsorption region 601 of the adsorption rotating wheel 60, so that the waste gas inlet pipe 61 can convey the organic waste gas to one side of the adsorption region 601 of the adsorption rotating wheel 60, one end of the net gas discharge pipe 62 is connected to the other side of the adsorption region 601 of the adsorption rotating wheel 60, the other end of the net gas discharge pipe 62 is connected to the chimney 80, and the net gas discharge pipe 62 is provided with a fan 621 (as shown in fig. 3 and 4), so that the adsorbed gas in the net gas discharge pipe 62 can be pushed into the chimney 80 through the fan 621 for discharge.
One side of the cooling region 602 of the sorption rotor 60 is connected to the cooling gas inlet conduit 63 for the gas to enter the cooling region 602 of the sorption rotor 60 for cooling use (as shown in figures 1 to 4), and the other side of the cooling zone 602 of the sorption rotor 60 is connected to one end of the cooling gas delivery pipe 64, and the other end of the cooling gas delivery pipe 64 is connected to one end of the second cold-side pipe 31 of the second heat exchanger 30, so as to convey the gas entering the cooling zone 602 of the adsorption rotor 60 into the second heat exchanger 30 for heat exchange (as shown in fig. 1 to 4), and furthermore, one end of the hot gas conveying pipeline 65 is connected to the other side of the desorption zone 603 of the adsorption rotor 60, and the other end of the hot gas delivery line 65 is connected to the other end of the second cold side line 31 of the second heat exchanger 30, the high-temperature hot gas heat-exchanged by the second heat exchanger 30 can be transferred to the desorption region 603 of the adsorption rotor 60 through the hot gas transfer line 65 for desorption.
The cooling zone 602 of the sorption rotor 60 has two embodiments, wherein in the first embodiment, the cooling air inlet line 63 connected to one side of the cooling zone 602 of the sorption rotor 60 is used for introducing fresh air or outside air (as shown in fig. 1), and the cooling of the cooling zone 602 of the sorption rotor 60 is provided by the fresh air or the outside air. The exhaust gas inlet pipe 61 of the second embodiment is provided with an exhaust gas communication pipe 611, and the other end of the exhaust gas communication pipe 611 is connected to the cooling gas inlet pipe 63 (as shown in fig. 2 and 4) so as to convey the exhaust gas in the exhaust gas inlet pipe 61 to the cooling zone 602 of the sorption rotor 60 for cooling through the exhaust gas communication pipe 611, and the exhaust gas communication pipe 611 is provided with an exhaust gas communication control valve 6111 so as to control the air volume of the exhaust gas communication pipe 611.
One end of the desorption concentrated gas line 66 is connected TO one side of the desorption region 603 of the adsorption rotor 60, and the other end of the desorption concentrated gas line 66 is connected TO one end of the first cold-side line 21 of the first heat exchanger 20, wherein the other end of the first cold-side line 21 of the first heat exchanger 20 is connected TO one end of the first cold-side transfer line 23, and the other end of the first cold-side transfer line 23 is connected TO the inlet 11 of the direct combustion type incinerator (TO)10, so that the desorption concentrated gas desorbed at a high temperature can be transferred into one end of the first cold-side line 21 of the first heat exchanger 20 through the desorption concentrated gas line 66, and can be transferred into the inlet 11 of the direct combustion type incinerator (TO)10 from the other end of the first cold-side line 21 of the first heat exchanger 20 (as shown in fig. 1 TO 4), so that the burner 101 of the direct combustion type incinerator (TO)10 can be pyrolyzed, so that volatile organic compounds can be reduced. The concentrated desorption gas line 66 is provided with a fan 661 to push and pull the concentrated desorption gas into one end of the first cold-side line 21 of the first heat exchanger 20.
Furthermore, the energy-saving single-runner cold-side bypass over-temperature control system of the present invention mainly has two embodiments, and the direct-fired incinerator (TO)10, the first heat exchanger 20, the second heat exchanger 30, the first cold-side delivery pipe 23, the adsorption runner 60 and the chimney 80 in the two embodiments are designed in the same way, so that the contents of the direct-fired incinerator (TO)10, the first heat exchanger 20, the second heat exchanger 30, the first cold-side delivery pipe 23, the adsorption runner 60 and the chimney 80 are not repeated, and please refer TO the above description.
The difference of the first embodiment (as shown in fig. 1 and fig. 2) is that a cold-side proportional damper 901 is additionally arranged between the desorption/concentration gas pipeline 66 and the first cold-side conveying pipeline 23, one end of the cold-side proportional damper 901 is connected to the desorption/concentration gas pipeline 66, and the other end of the cold-side proportional damper 901 is connected to the first cold-side conveying pipeline 23, so as to regulate the air volume of the desorption/concentration gas pipeline 66 and the first cold-side conveying pipeline 23 through the cold-side proportional damper 901, therefore, when the concentration of Volatile Organic Compounds (VOCs) in the first cold-side conveying pipeline 23 becomes high, part of the desorption/concentration gas in the desorption/concentration gas pipeline 66 can be conveyed into the first cold-side conveying pipeline 23 through the cold-side proportional damper 901, so that the desorption/concentration gas in the first cold-side conveying pipeline 23 can be mixed with part of the desorption/concentration gas in the desorption/concentration gas pipeline 66 again, the temperature of the concentrated desorption gas in the concentrated desorption gas pipeline 66 can be reduced by the concentrated desorption gas in the first cold side conveying pipeline 23, so that when the concentration of Volatile Organic Compounds (VOCs) is increased, the air volume can be adjusted and controlled by the cold side proportion air door 901, the heat recovery amount or concentration can be adjusted, and the direct-fired incinerator (TO)10 can be prevented from being over-heated due TO too high incinerator temperature and even being shut down when organic waste gas is treated.
The difference of the second embodiment (as shown in fig. 3 and fig. 4) is that a cold-side proportional damper 904 is added to the desorption concentrated gas pipeline 66, and the other end of the cold-side proportional damper 904 is provided for the entry of external air, wherein the external air may be fresh air or other gas, so as to regulate the air volume of the desorption concentrated gas pipeline 66 through the cold-side proportional damper 904. In addition, when the desorption/concentration gas pipe 66 is provided with the fan 661, the cold-side proportional damper 904 is provided upstream of the fan 661, i.e., at the inlet of the fan 661, to form a negative pressure state, so that the outside air can be introduced through the cold-side proportional damper 904. Therefore, when the desorption concentrated gas generated by the desorption zone 603 of the adsorption rotor 60 enters the desorption concentrated gas pipeline 66 and the temperature or the concentration in the desorption concentrated gas pipeline 66 becomes higher, the temperature of the desorption concentrated gas can be adjusted by inputting the outside air through the other end of the cold-side proportional air door 904, so that the desorption concentrated gas in the desorption concentrated gas pipeline 66 can achieve the effect of reducing the temperature or the concentration.
The energy-saving single-runner cold-side bypass over-temperature control method of the invention is mainly used for organic waste gas treatment systems, and comprises a combined design of a direct-fired incinerator (TO)10, a first heat exchanger 20, a second heat exchanger 30, a first cold-side conveying pipeline 23, an adsorption runner 60 and a chimney 80 (as shown in fig. 1 TO 4), wherein the first heat exchanger 20 is provided with a first cold-side pipeline 21 and a first hot-side pipeline 22, the second heat exchanger 30 is provided with a second cold-side pipeline 31 and a second hot-side pipeline 32, one end of the first cold-side conveying pipeline 23 is connected with the other end of the first cold-side pipeline 21, and the other end of the first cold-side conveying pipeline 23 is connected with an inlet 11 of the direct-fired incinerator (TO) 10. The direct-fired incinerator (TO)10 is provided with a burner 101 and a hearth 102, the burner 101 is communicated with the hearth 102, the first heat exchanger 20 and the second heat exchanger 30 are respectively arranged in the hearth 102 of the direct-fired incinerator (TO)10, the direct-fired incinerator (TO)10 is provided with an inlet 11 and an outlet 12 (as shown in fig. 1 TO 4), the inlet 11 is arranged at the burner 101, the merging port 11 is connected with the other end of the first cold-side pipeline 21 of the first heat exchanger 20, the outlet 12 is arranged at the hearth 102, and the outlet 12 is connected TO the chimney 80, so that organic waste gas can enter the burner 101 from the inlet 11 TO be combusted, and combusted gas can pass through the hearth 102 and be discharged TO the chimney 80 from the outlet 12 TO be discharged, thereby having the energy-saving effect.
The adsorption rotor 60 of the present invention is provided with an adsorption zone 601, a cooling zone 602 and a desorption zone 603, and the adsorption rotor 60 is connected to a waste gas inlet line 61, a clean gas discharge line 62, a cooling gas inlet line 63, a cooling gas delivery line 64, a hot gas delivery line 65 and a desorption concentrated gas line 66 (as shown in fig. 1 to 4). Wherein the adsorption rotor 60 is a zeolite concentration rotor or a concentration rotor made of other materials.
The main steps of the control method of the present invention (as shown in fig. 5) include: step S100 inputs gas to be adsorbed: the exhaust gas is fed to one side of the adsorption zone 601 of the adsorption rotor 60 through the other end of the exhaust gas inlet line 61. After the step S100 is completed, the next step S110 is performed.
The next step is that step S110 is carried out to adsorb the rotary wheel: after being adsorbed by the adsorption zone 601 of the adsorption rotor 60, the adsorbed gas is discharged from the other side of the adsorption zone 601 of the adsorption rotor 60 through the other end of the clean gas discharge line 62. After the step S110 is completed, the next step S120 is performed.
The other side of the adsorption region 601 of the adsorption rotor 60 in the step S110 is connected to the clean gas discharge pipe 62 to be connected to the chimney 80 through the other end of the clean gas discharge pipe 62, and the clean gas discharge pipe 62 is provided with a fan 621 (as shown in fig. 3 and 4), so that the adsorbed gas in the clean gas discharge pipe 62 can be pushed into the chimney 80 by the fan 621 for discharge.
The next step proceeds to step S120 of inputting cooling gas: the cooling gas is supplied to the cooling zone 602 of the sorption rotor 60 for cooling by the other end of the cooling gas inlet conduit 63, and the cooling gas passing through the cooling zone 602 of the sorption rotor 60 is supplied to one end of the second cold-side conduit 31 of the second heat exchanger 30 by the other end of the cooling gas supply conduit 64. After the step S120 is completed, the next step S130 is performed.
In the above step S120, the cooling area 602 of the sorption rotor 60 has two embodiments, wherein in the first embodiment, the cooling air inlet pipeline 63 connected to one side of the cooling area 602 of the sorption rotor 60 is used for introducing fresh air or external air (as shown in fig. 1), and the cooling area 602 of the sorption rotor 60 is provided by the fresh air or the external air for cooling. The exhaust gas inlet pipe 61 of the second embodiment is provided with an exhaust gas communication pipe 611, and the other end of the exhaust gas communication pipe 611 is connected to the cooling gas inlet pipe 63 (as shown in fig. 2 and 4) so as to convey the exhaust gas in the exhaust gas inlet pipe 61 to the cooling zone 602 of the sorption rotor 60 for cooling through the exhaust gas communication pipe 611, and the exhaust gas communication pipe 611 is provided with an exhaust gas communication control valve 6111 for controlling the air volume of the exhaust gas communication pipe 611.
The next step, step S130, is to deliver hot gas desorption: hot gas is delivered to the desorption zone 603 of the adsorption rotor 60 for desorption through a hot gas delivery line 65 connected to the other end of the second cold side line 31 of the second heat exchanger 30, and desorption concentrated gas is delivered to one end of the first cold side line 21 of the first heat exchanger 20 through the other end of the desorption concentrated gas line 66. After the step S130 is completed, the next step S140 is performed.
The desorption concentrated gas pipeline 66 in the step S130 is provided with a fan 661 (as shown in fig. 3 and 4) to push and pull the desorption concentrated gas into the first cold-side pipeline 21 of the first heat exchanger 20.
The next step, step S140, is to desorb the concentrated gas delivery: the desorbed concentrated gas is further transferred TO the inlet 11 of the direct combustion incinerator (TO)10 through the first cold-side transfer pipe 23 connected TO the other end of the first cold-side pipe 21 of the first heat exchanger 20. After the step S140 is completed, the next step S150 is performed.
Next, the burned gas is delivered in step S150: the burned gas generated by the combustion of the burner 101 of the direct combustion type incinerator (TO)10 is transferred TO one end of the second hot side pipe 32 of the second heat exchanger 30, then transferred TO one end of the first hot side pipe 22 of the first heat exchanger 20 by the other end of the second hot side pipe 32 of the second heat exchanger 30, and finally transferred TO the outlet 12 of the direct combustion type incinerator (TO)10 by the other end of the first hot side pipe 22 of the first heat exchanger 20. After the step S150 is completed, the next step S160 is performed.
The burner 101 of the direct-fired incinerator (TO)10 in the step S150 can firstly deliver the high-temperature burned gas TO one side of the second hot-side pipeline 32 of the second heat exchanger 30 for heat exchange (as shown in fig. 1), then deliver the high-temperature burned gas TO one side of the first hot-side pipeline 22 of the first heat exchanger 20 again from the other side of the second hot-side pipeline 32 of the second heat exchanger 30 for heat exchange, finally deliver the high-temperature burned gas TO the outlet 12 of the furnace 102 from the other side of the first hot-side pipeline 22 of the first heat exchanger 20, and deliver the high-temperature burned gas TO the chimney 80 from the outlet 12 of the furnace 102 for discharge through the chimney 80.
Step S160, cold side proportional damper adjustment, proceeds as follows: a cold-side proportional damper 901 is disposed between the desorption concentrated gas pipeline 66 and the first cold-side conveying pipeline 23, so as to regulate and control the air volume of the desorption concentrated gas pipeline 66 and the first cold-side conveying pipeline 23 through the cold-side proportional damper 901.
In the step S160, one end of the cold-side proportional damper 901 is connected to the desorption concentrated gas pipe 66, and the other end of the cold-side proportional damper 901 is connected to the first cold-side conveying pipe 23 (as shown in fig. 1), so as to regulate and control the air flow of the desorption concentrated gas pipe 66 and the first cold-side conveying pipe 23 through the cold-side proportional damper 901, when the concentration of Volatile Organic Compounds (VOCs) in the first cold-side conveying pipe 23 becomes high, part of the desorption concentrated gas in the desorption concentrated gas pipe 66 can be conveyed into the first cold-side conveying pipe 23 through the cold-side proportional damper 901, so that the desorption concentrated gas in the first cold-side conveying pipe 23 and part of the desorption concentrated gas in the desorption concentrated gas pipe 66 can be mixed again, and part of the desorption concentrated gas in the desorption concentrated gas pipe 66 with a lower temperature can cool the desorption concentrated gas in the first cold-side conveying pipe 23 with a higher temperature, therefore, when the concentration of Volatile Organic Compounds (VOCs) becomes high, the air volume can be controlled by the cold-side proportional damper 901 TO have the effect of adjusting the heat recovery amount or concentration, so that the direct-fired incinerator (TO)10 can be prevented from being overheated due TO too high furnace temperature and even being shut down when organic waste gas is treated.
Furthermore, the energy-saving single-runner cold-side bypass over-temperature control method of the present invention mainly has four embodiments, and the first embodiment (as shown in fig. 5) includes step S100 of inputting the gas to be adsorbed, step S110 of adsorbing the runner for adsorption, step S120 of inputting the cooling gas, step S130 of delivering the hot gas for desorption, step S140 of desorbing the concentrated gas for delivery, step S150 of incinerating the gas, and step S160 of adjusting the cold-side proportional damper, which have been already mentioned above, please refer to the above description.
In the second embodiment (as shown in fig. 6), the gas to be adsorbed is input in step S200, the adsorption runner is used for adsorption in step S210, the cooling gas is input in step S220, the hot gas is input in step S230 for desorption, the concentrated gas is desorbed in step S240 for transportation, and the gas is transported after incineration in step S250, as well as the gas to be adsorbed is input in step S300, the adsorption runner is used for adsorption in step S310, the cooling gas is input in step S320, the hot gas is transmitted in step S330 for desorption, the concentrated gas is desorbed in step S340 for transportation, and the gas is transported after incineration in step S350 in the third embodiment (as shown in fig. 7), and the gas to be adsorbed is input in step S400, the adsorption runner is used for adsorption in step S410, the cooling gas is input in step S420, the hot gas is transmitted in step S430 for desorption, the concentrated gas is desorbed in step S440 for transportation, and the gas is transported after incineration in step S450, which the gas to be adsorbed is input in step S100, the gas to be adsorbed in the first embodiment (as shown in fig. 1), The same design of adsorption by the adsorption rotor in step S110, cooling gas input in step S120, hot gas desorption in step S130, concentrated gas desorption in step S140, and gas delivery after incineration in step S150 is different only in the content of gas delivery after incineration in step S150 and cold side proportional damper control in step S160.
Therefore, the same contents as those of the gas to be adsorbed input in step S100, the adsorption by the adsorption rotor in step S110, the cooling gas input in step S120, the hot gas desorption in step S130, and the concentrated gas desorption in step S140 are not repeated, and please refer to the above description. The following description will be made with respect to the transport of the burned gas in step S250 and the cold-side proportional damper control in step S260 in the second embodiment (shown in fig. 6), the transport of the burned gas in step S350 and the cold-side proportional damper control in step S360 in the third embodiment (shown in fig. 7), and the transport of the burned gas in step S450 and the cold-side proportional damper control in step S460 in the fourth embodiment (shown in fig. 8).
The difference of the second embodiment (as shown in fig. 6) is the gas delivery after incineration in step S250: the burned gas generated by the combustion of the burner 101 of the direct combustion type incinerator (TO)10 is transferred TO one end of the first hot side pipe 22 of the first heat exchanger 20, transferred TO one end of the second hot side pipe 32 of the second heat exchanger 30 from the other end of the first hot side pipe 22 of the first heat exchanger 20, and transferred TO the outlet 12 of the direct combustion type incinerator (TO)10 from the other end of the second hot side pipe 32 of the second heat exchanger 30.
In the step S250, the burner 101 of the direct-fired incinerator (TO)10 can firstly deliver the incinerated high-temperature gas TO one side of the first hot-side pipeline 22 of the first heat exchanger 20 for heat exchange (as shown in fig. 2), and the incinerated high-temperature gas is then delivered TO one side of the second hot-side pipeline 32 of the second heat exchanger 30 for heat exchange by the other side of the first hot-side pipeline 22 of the first heat exchanger 20, and then the incinerated high-temperature gas is delivered TO the outlet 12 of the furnace 102 by the other side of the second hot-side pipeline 32 of the second heat exchanger 30, and then delivered TO the chimney 80 by the outlet 12 of the furnace 102, so as TO be discharged through the chimney 80.
And step S260 cold side proportional damper regulation: a cold side proportion damper 901 is arranged between the first desorption concentrated gas pipeline 66 and the first cold side conveying pipeline 23, so as to regulate and control the air volume of the first desorption concentrated gas pipeline 66 and the first cold side conveying pipeline 23 through the cold side proportion damper 901.
In the step S260, one end of the cold-side proportional damper 901 is connected to the desorption concentrated gas pipe 66, and the other end of the cold-side proportional damper 901 is connected to the first cold-side delivery pipe 23 (as shown in fig. 2), so as to regulate and control the air flow of the desorption concentrated gas pipe 66 and the first cold-side delivery pipe 23 through the cold-side proportional damper 901, when the concentration of Volatile Organic Compounds (VOCs) in the first cold-side delivery pipe 23 becomes high, part of the desorption concentrated gas in the desorption concentrated gas pipe 66 can be delivered into the first cold-side delivery pipe 23 through the cold-side proportional damper 901, so that the desorption concentrated gas in the first cold-side delivery pipe 23 can be mixed with part of the desorption concentrated gas in the desorption concentrated gas pipe 66 again, and part of the desorption concentrated gas in the desorption concentrated gas pipe 66 with a lower temperature can cool the desorption concentrated gas in the first cold-side delivery pipe 23 with a higher temperature, therefore, when the concentration of Volatile Organic Compounds (VOCs) becomes high, the air volume can be controlled by the cold-side proportional damper 901 TO have the effect of adjusting the heat recovery amount or concentration, so that the direct-fired incinerator (TO)10 can be prevented from being overheated due TO too high furnace temperature and even being shut down when organic waste gas is treated.
The difference of the third embodiment (as shown in fig. 7) is the gas delivery after incineration in step S350: the burned gas generated by the combustion of the burner 101 of the direct combustion type incinerator (TO)10 is transferred TO one end of the second hot side pipe 32 of the second heat exchanger 30, is transferred TO one end of the first hot side pipe 22 of the first heat exchanger 20 from the other end of the second hot side pipe 32 of the second heat exchanger 30, and is transferred TO the outlet 12 of the direct combustion type incinerator (TO)10 from the other end of the first hot side pipe 22 of the first heat exchanger 20.
In the step S350, the burner 101 of the direct combustion type incinerator (TO)10 can firstly deliver the incinerated high-temperature gas TO one side of the second hot-side pipeline 32 of the second heat exchanger 30 for heat exchange, and then deliver the incinerated high-temperature gas TO one side of the first hot-side pipeline 22 of the first heat exchanger 20 for heat exchange from the other side of the second hot-side pipeline 32 of the second heat exchanger 30 (as shown in fig. 3), and deliver the incinerated high-temperature gas TO the outlet 12 of the furnace 102 from the other side of the first hot-side pipeline 22 of the first heat exchanger 20, and deliver the incinerated high-temperature gas TO the chimney 80 from the outlet 12 of the furnace 102 for discharge through the chimney 80.
And step S360 cold side proportional damper regulation: a cold side proportional damper 904 is disposed on the desorption concentrated gas pipeline 66, and the other end of the cold side proportional damper 904 is used for external air to enter, so as to regulate the air volume of the desorption concentrated gas pipeline 66 through the cold side proportional damper 904.
In the step S360, the other end of the cold-side proportional damper 904 is used for allowing external air to enter (as shown in fig. 3), wherein the external air may be fresh air or other gas, so as to regulate the air volume of the first desorption/concentration gas pipeline 66 through the cold-side proportional damper 904. In addition, when the desorption/concentration gas pipe 66 is provided with the fan 661, the cold-side proportional damper 904 is provided upstream of the fan 661, i.e., at the inlet of the fan 661, to form a negative pressure state, so that the outside air can be introduced through the cold-side proportional damper 904. Therefore, after the concentrated desorption gas generated by the desorption region 603 of the first adsorption rotor 60 enters the first concentrated desorption gas pipeline 66, and the temperature or the concentration in the first concentrated desorption gas pipeline 66 becomes higher, the temperature can be adjusted by inputting the outside air through the other end of the cold-side proportional air door 904, so that the concentrated desorption gas in the first concentrated desorption gas pipeline 66 can achieve the effect of reducing the temperature or the concentration.
Furthermore, the difference of the fourth embodiment (as shown in FIG. 8) is the gas delivery after incineration in step S450: the burned gas generated by the combustion of the burner 101 of the direct combustion type incinerator (TO)10 is transferred TO one end of the first hot side pipe 22 of the first heat exchanger 20, transferred TO one end of the second hot side pipe 32 of the second heat exchanger 30 from the other end of the first hot side pipe 22 of the first heat exchanger 20, and transferred TO the outlet 12 of the direct combustion type incinerator (TO)10 from the other end of the second hot side pipe 32 of the second heat exchanger 30.
In the step S450, the burner 101 of the direct combustion incinerator (TO)10 can firstly deliver the incinerated high-temperature gas TO one side of the first hot-side pipeline 22 of the first heat exchanger 20 for heat exchange (as shown in fig. 4), and the incinerated high-temperature gas is then delivered TO one side of the second hot-side pipeline 32 of the second heat exchanger 30 for heat exchange by the other side of the first hot-side pipeline 22 of the first heat exchanger 20, and then the incinerated high-temperature gas is delivered TO the outlet 12 of the furnace 102 by the other side of the second hot-side pipeline 32 of the second heat exchanger 30, and then is delivered TO the chimney 80 by the outlet 12 of the furnace 102 for discharge through the chimney 80.
And step S460 cold side proportional damper adjustment: a cold side proportional damper 904 is disposed on the desorption concentrated gas pipeline 66, and the other end of the cold side proportional damper 904 is used for external air to enter, so as to regulate the air volume of the desorption concentrated gas pipeline 66 through the cold side proportional damper 904.
In the above step S460, the other end of the cold-side proportional damper 904 is used for allowing external air to enter (as shown in fig. 4), wherein the external air may be fresh air or other gas, so as to regulate the air volume of the first desorption concentrated gas pipeline 66 through the cold-side proportional damper 904. In addition, when the desorption/concentration gas pipe 66 is provided with the fan 661, the cold-side proportional damper 904 is provided upstream of the fan 661, i.e., at the inlet of the fan 661, to form a negative pressure state, so that the outside air can be introduced through the cold-side proportional damper 904. Therefore, after the concentrated desorption gas generated by the desorption region 603 of the first adsorption rotor 60 enters the first concentrated desorption gas pipeline 66, and the temperature or the concentration in the first concentrated desorption gas pipeline 66 becomes higher, the temperature can be adjusted by inputting the outside air through the other end of the cold-side proportional air door 904, so that the concentrated desorption gas in the first concentrated desorption gas pipeline 66 can achieve the effect of reducing the temperature or the concentration.
From the above detailed description, those skilled in the art will be able to understand that the above-described effects of the present invention are achieved in accordance with the provisions of the patent statutes.
The above-mentioned embodiments are only used to illustrate the implementation status of the present invention and to explain the technical features of the present invention, and are not used to limit the protection scope of the present invention. Any modifications or similar modifications that can be easily made by the skilled person fall within the scope of the claims of the present invention, which shall be subject to the protection scope of the present patent application.
Claims (16)
1. An energy-saving single runner cold side bypass over-temperature control system, characterized by comprising:
the direct-fired incinerator (TO) is provided with a furnace end and a hearth, the furnace end is communicated with the hearth, the direct-fired incinerator (TO) is provided with an inlet and an outlet, the inlet is arranged at the furnace end, and the outlet is arranged at the hearth;
a first heat exchanger, arranged in the furnace of the direct-fired incinerator (TO), provided with a first cold-side pipeline and a first hot-side pipeline;
a second heat exchanger, which is arranged in the furnace chamber of the direct-fired incinerator (TO) and is provided with a second cold-side pipeline and a second hot-side pipeline;
a first cold side transfer pipe having one end connected TO the other end of the first cold side pipe, the other end of the first cold side transfer pipe being connected TO an inlet of the direct combustion incinerator (TO);
the adsorption rotating wheel is provided with an adsorption area, a cooling area and a desorption area, the adsorption rotating wheel is connected with a waste gas inlet pipeline, a clean gas discharge pipeline, a cooling gas inlet pipeline, a cooling gas conveying pipeline, a hot gas conveying pipeline and a desorption concentrated gas pipeline, one end of the waste gas inlet pipeline is connected to one side of the adsorption area of the adsorption rotating wheel, one end of the clean gas discharge pipeline is connected with the other side of the adsorption area of the adsorption rotating wheel, one end of the cooling gas inlet pipeline is connected with one side of the cooling area of the adsorption rotating wheel, one end of the cooling gas conveying pipeline is connected with the other side of the cooling area of the adsorption rotating wheel, the other end of the cooling gas conveying pipeline is connected with one end of a second cold side pipeline of the second heat exchanger, and one end of the hot gas conveying pipeline is connected with the other side of the desorption area of the adsorption rotating wheel, the other end of the hot gas conveying pipeline is connected with the other end of a second cold side pipeline of the second heat exchanger, one end of the desorption concentrated gas pipeline is connected with one side of a desorption area of the adsorption rotating wheel, and the other end of the desorption concentrated gas pipeline is connected with one end of a first cold side pipeline of the first heat exchanger;
the other end of the purified gas discharge pipeline is connected with the chimney; and
and one end of the cold side proportion air door is connected with the desorption concentrated gas pipeline, and the other end of the cold side proportion air door is connected with the first cold side conveying pipeline.
2. An energy-saving single runner cold side bypass over-temperature control system, characterized by comprising:
the direct-fired incinerator (TO) is provided with a furnace end and a hearth, the furnace end is communicated with the hearth, the direct-fired incinerator (TO) is provided with an inlet and an outlet, the inlet is arranged at the furnace end, and the outlet is arranged at the hearth;
a first heat exchanger, arranged in the furnace of the direct-fired incinerator (TO), provided with a first cold-side pipeline and a first hot-side pipeline;
a second heat exchanger, arranged in the furnace chamber of the direct-fired incinerator (TO), provided with a second cold-side pipeline and a second hot-side pipeline;
a first cold side transfer pipe having one end connected TO the other end of the first cold side pipe, the other end of the first cold side transfer pipe being connected TO an inlet of the direct combustion incinerator (TO);
the adsorption rotating wheel is provided with an adsorption area, a cooling area and a desorption area, the adsorption rotating wheel is connected with a waste gas inlet pipeline, a clean gas discharge pipeline, a cooling gas inlet pipeline, a cooling gas conveying pipeline, a hot gas conveying pipeline and a desorption concentrated gas pipeline, one end of the waste gas inlet pipeline is connected to one side of the adsorption area of the adsorption rotating wheel, one end of the clean gas discharge pipeline is connected with the other side of the adsorption area of the adsorption rotating wheel, one end of the cooling gas inlet pipeline is connected with one side of the cooling area of the adsorption rotating wheel, one end of the cooling gas conveying pipeline is connected with the other side of the cooling area of the adsorption rotating wheel, the other end of the cooling gas conveying pipeline is connected with one end of a second cold side pipeline of the second heat exchanger, and one end of the hot gas conveying pipeline is connected with the other side of the desorption area of the adsorption rotating wheel, the other end of the hot gas conveying pipeline is connected with the other end of a second cold side pipeline of the second heat exchanger, one end of the desorption concentrated gas pipeline is connected with one side of a desorption area of the adsorption rotating wheel, and the other end of the desorption concentrated gas pipeline is connected with one end of a first cold side pipeline of the first heat exchanger;
the other end of the purified gas discharge pipeline is connected with the chimney; and
and one end of the cold side proportion air door is connected with the desorption concentrated gas pipeline, and the other end of the cold side proportion air door is used for allowing external air to enter.
3. Energy-saving single-runner cold-side bypass over-temperature control system according TO claim 1 or 2, characterized in that the outlet of the direct-fired incinerator (TO) is further connected TO the chimney.
4. The economized single-spool cold-side bypass over-temperature control system as claimed in claim 1 or 2 wherein said cooling air intake conduit is further accessible for fresh or outside air.
5. The energy-saving single-runner cold-side bypass over-temperature control system as claimed in claim 1 or 2, wherein the exhaust gas inlet pipeline is further provided with an exhaust gas communication pipeline, the exhaust gas communication pipeline is connected with the cooling gas inlet pipeline, and the exhaust gas communication pipeline is further provided with an exhaust gas communication control valve to control the air volume of the exhaust gas communication pipeline.
6. The energy-saving single-runner cold-side bypass over-temperature control system as claimed in claim 1 or 2, wherein the desorption concentrated gas pipeline is further provided with a fan.
7. The economized single-spool cold-side bypass over-temperature control system as claimed in claim 1 or 2, wherein said purge gas discharge line is further provided with a fan.
8. An energy-saving single-runner cold-side bypass over-temperature control method is mainly used for an organic waste gas treatment system and is provided with a direct-fired incinerator (TO), a first heat exchanger, a second heat exchanger, a first cold-side conveying pipeline, an adsorption runner and a chimney, wherein the direct-fired incinerator (TO) is provided with a furnace end and a furnace chamber, the furnace end is communicated with the furnace chamber, the direct-fired incinerator (TO) is provided with an inlet and an outlet, the inlet is arranged at the furnace end, the outlet is arranged at the furnace chamber, the first heat exchanger is provided with a first cold-side pipeline and a first hot-side pipeline, the second heat exchanger is provided with a second cold-side pipeline and a second hot-side pipeline, one end of the first cold-side conveying pipeline is connected with the other end of the first cold-side pipeline, the other end of the first cold-side conveying pipeline is connected with the inlet of the direct-fired incinerator (TO), the adsorption rotating wheel is provided with an adsorption area, a cooling area and a desorption area, the adsorption rotating wheel is connected with a waste gas inlet pipeline, a clean gas discharge pipeline, a cooling gas inlet pipeline, a cooling gas conveying pipeline, a hot gas conveying pipeline and a desorption concentrated gas pipeline, and the control method mainly comprises the following steps:
input of gas to be adsorbed: waste gas is sent to one side of the adsorption area of the adsorption runner through the other end of the waste gas inlet pipeline;
the adsorption runner carries out adsorption: after the gas is adsorbed by the adsorption area of the adsorption rotating wheel, the gas after adsorption is output by the other side of the adsorption area of the adsorption rotating wheel through the other end of the purified gas discharge pipeline;
inputting cooling gas: conveying cooling gas to a cooling area of the adsorption runner for cooling through the other end of the cooling gas inlet pipeline, and conveying the cooling gas passing through the cooling area of the adsorption runner to one end of a second cold-side pipeline of the second heat exchanger through the other end of the cooling gas conveying pipeline;
conveying hot gas for desorption: 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 second cold side pipeline of the second heat exchanger, and desorption concentrated gas is conveyed to one end of the first cold side pipeline of the first heat exchanger through the other end of the desorption concentrated gas pipeline;
and (3) desorption and concentrated gas conveying: the desorbed concentrated gas is conveyed TO the inlet of the direct-fired incinerator (TO) through a first cold-side conveying pipeline connected with the other end of the first cold-side pipeline of the first heat exchanger;
conveying gas after incineration: conveying the incinerated gas generated by burning the burner of the direct-fired incinerator (TO) TO one end of a second hot side pipeline of the second heat exchanger, then conveying the incinerated gas TO one end of a first hot side pipeline of the first heat exchanger from the other end of the second hot side pipeline of the second heat exchanger, and finally conveying the incinerated gas TO an outlet of the direct-fired incinerator (TO) from the other end of the first hot side pipeline of the first heat exchanger; and
and (3) regulating and controlling a cold-side proportional air door: a cold side proportion air door is arranged between the desorption concentrated gas pipeline and the first cold side conveying pipeline so as to regulate and control the air volume of the desorption concentrated gas pipeline and the first cold side conveying pipeline through the cold side proportion air door.
9. An energy-saving single-runner cold-side bypass over-temperature control method is mainly used for an organic waste gas treatment system and is provided with a direct-fired incinerator (TO), a first heat exchanger, a second heat exchanger, a first cold-side conveying pipeline, an adsorption runner and a chimney, wherein the direct-fired incinerator (TO) is provided with a furnace end and a furnace chamber, the furnace end is communicated with the furnace chamber, the direct-fired incinerator (TO) is provided with an inlet and an outlet, the inlet is arranged at the furnace end, the outlet is arranged at the furnace chamber, the first heat exchanger is provided with a first cold-side pipeline and a first hot-side pipeline, the second heat exchanger is provided with a second cold-side pipeline and a second hot-side pipeline, one end of the first cold-side conveying pipeline is connected with the other end of the first cold-side pipeline, the other end of the first cold-side conveying pipeline is connected with the inlet of the direct-fired incinerator (TO), the adsorption rotating wheel is provided with an adsorption area, a cooling area and a desorption area, the adsorption rotating wheel is connected with a waste gas inlet pipeline, a clean gas discharge pipeline, a cooling gas inlet pipeline, a cooling gas conveying pipeline, a hot gas conveying pipeline and a desorption concentrated gas pipeline, and the control method mainly comprises the following steps:
input of gas to be adsorbed: waste gas is sent to one side of the adsorption area of the adsorption runner through the other end of the waste gas inlet pipeline;
the adsorption runner carries out adsorption: after the gas is adsorbed by the adsorption area of the adsorption rotating wheel, the gas after adsorption is output by the other side of the adsorption area of the adsorption rotating wheel through the other end of the purified gas discharge pipeline;
inputting cooling gas: conveying cooling gas to a cooling area of the adsorption runner for cooling through the other end of the cooling gas inlet pipeline, and conveying the cooling gas passing through the cooling area of the adsorption runner to one end of a second cold-side pipeline of the second heat exchanger through the other end of the cooling gas conveying pipeline;
conveying hot gas for desorption: 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 second cold side pipeline of the second heat exchanger, and desorption concentrated gas is conveyed to one end of the first cold side pipeline of the first heat exchanger through the other end of the desorption concentrated gas pipeline;
and (3) desorption and concentrated gas conveying: the desorbed concentrated gas is conveyed TO the inlet of the direct-fired incinerator (TO) through a first cold-side conveying pipeline connected with the other end of the first cold-side pipeline of the first heat exchanger;
conveying gas after incineration: conveying the incinerated gas generated by the combustion of the burner of the direct-fired incinerator (TO) TO one end of a first hot-side pipeline of the first heat exchanger, conveying the incinerated gas TO one end of a second hot-side pipeline of the second heat exchanger from the other end of the first hot-side pipeline of the first heat exchanger, and conveying the incinerated gas TO the outlet of the direct-fired incinerator (TO) from the other end of the second hot-side pipeline of the second heat exchanger; and
and (3) regulating and controlling a cold-side proportional air door: a cold side proportion air door is arranged between the desorption concentrated gas pipeline and the first cold side conveying pipeline so as to regulate and control the air volume of the desorption concentrated gas pipeline and the first cold side conveying pipeline through the cold side proportion air door.
10. An energy-saving single-runner cold-side bypass over-temperature control method is mainly used for an organic waste gas treatment system and is provided with a direct-fired incinerator (TO), a first heat exchanger, a second heat exchanger, a first cold-side conveying pipeline, an adsorption runner and a chimney, wherein the direct-fired incinerator (TO) is provided with a furnace end and a furnace chamber, the furnace end is communicated with the furnace chamber, the direct-fired incinerator (TO) is provided with an inlet and an outlet, the inlet is arranged at the furnace end, the outlet is arranged at the furnace chamber, the first heat exchanger is provided with a first cold-side pipeline and a first hot-side pipeline, the second heat exchanger is provided with a second cold-side pipeline and a second hot-side pipeline, one end of the first cold-side conveying pipeline is connected with the other end of the first cold-side pipeline, the other end of the first cold-side conveying pipeline is connected with the inlet of the direct-fired incinerator (TO), the adsorption rotating wheel is provided with an adsorption area, a cooling area and a desorption area, the adsorption rotating wheel is connected with a waste gas inlet pipeline, a clean gas discharge pipeline, a cooling gas inlet pipeline, a cooling gas conveying pipeline, a hot gas conveying pipeline and a desorption concentrated gas pipeline, and the control method mainly comprises the following steps:
input of gas to be adsorbed: waste gas is sent to one side of the adsorption area of the adsorption runner through the other end of the waste gas inlet pipeline;
the adsorption runner carries out adsorption: after the gas is adsorbed by the adsorption area of the adsorption rotating wheel, the gas after adsorption is output by the other side of the adsorption area of the adsorption rotating wheel through the other end of the purified gas discharge pipeline;
inputting cooling gas: conveying cooling gas to a cooling area of the adsorption runner for cooling through the other end of the cooling gas inlet pipeline, and conveying the cooling gas passing through the cooling area of the adsorption runner to one end of a second cold-side pipeline of the second heat exchanger through the other end of the cooling gas conveying pipeline;
conveying hot gas for desorption: 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 second cold side pipeline of the second heat exchanger, and desorption concentrated gas is conveyed to one end of the first cold side pipeline of the first heat exchanger through the other end of the desorption concentrated gas pipeline;
and (3) desorption and concentrated gas conveying: the desorbed concentrated gas is conveyed TO the inlet of the direct-fired incinerator (TO) through a first cold-side conveying pipeline connected with the other end of the first cold-side pipeline of the first heat exchanger;
conveying gas after incineration: conveying the incinerated gas generated by burning the burner of the direct-fired incinerator (TO) TO one end of a second hot side pipeline of the second heat exchanger, then conveying the incinerated gas TO one end of a first hot side pipeline of the first heat exchanger from the other end of the second hot side pipeline of the second heat exchanger, and finally conveying the incinerated gas TO an outlet of the direct-fired incinerator (TO) from the other end of the first hot side pipeline of the first heat exchanger; and
and (3) regulating and controlling a cold-side proportional air door: and a cold side proportion air door is arranged on the desorption concentrated gas pipeline, and the other end of the cold side proportion air door is used for allowing external air to enter so as to regulate and control the air volume of the desorption concentrated gas pipeline through the cold side proportion air door.
11. An energy-saving single-runner cold-side bypass over-temperature control method is mainly used for an organic waste gas treatment system and is provided with a direct-fired incinerator (TO), a first heat exchanger, a second heat exchanger, a first cold-side conveying pipeline, an adsorption runner and a chimney, wherein the direct-fired incinerator (TO) is provided with a furnace end and a furnace chamber, the furnace end is communicated with the furnace chamber, the direct-fired incinerator (TO) is provided with an inlet and an outlet, the inlet is arranged at the furnace end, the outlet is arranged at the furnace chamber, the first heat exchanger is provided with a first cold-side pipeline and a first hot-side pipeline, the second heat exchanger is provided with a second cold-side pipeline and a second hot-side pipeline, one end of the first cold-side conveying pipeline is connected with the other end of the first cold-side pipeline, the other end of the first cold-side conveying pipeline is connected with the inlet of the direct-fired incinerator (TO), the adsorption rotating wheel is provided with an adsorption area, a cooling area and a desorption area, the adsorption rotating wheel is connected with a waste gas inlet pipeline, a clean gas discharge pipeline, a cooling gas inlet pipeline, a cooling gas conveying pipeline, a hot gas conveying pipeline and a desorption concentrated gas pipeline, and the control method mainly comprises the following steps:
input of gas to be adsorbed: waste gas is sent to one side of the adsorption area of the adsorption runner through the other end of the waste gas inlet pipeline;
the adsorption runner carries out adsorption: after the gas is adsorbed by the adsorption area of the adsorption rotating wheel, the gas after adsorption is output by the other side of the adsorption area of the adsorption rotating wheel through the other end of the purified gas discharge pipeline;
inputting cooling gas: conveying cooling gas to a cooling area of the adsorption runner for cooling through the other end of the cooling gas inlet pipeline, and conveying the cooling gas passing through the cooling area of the adsorption runner to one end of a second cold-side pipeline of the second heat exchanger through the other end of the cooling gas conveying pipeline;
conveying hot gas for desorption: 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 second cold side pipeline of the second heat exchanger, and desorption concentrated gas is conveyed to one end of the first cold side pipeline of the first heat exchanger through the other end of the desorption concentrated gas pipeline;
and (3) desorption and concentrated gas conveying: the desorbed concentrated gas is conveyed TO the inlet of the direct-fired incinerator (TO) through a first cold-side conveying pipeline connected with the other end of the first cold-side pipeline of the first heat exchanger;
conveying gas after incineration: conveying the incinerated gas generated by the combustion of the burner of the direct-fired incinerator (TO) TO one end of a first hot-side pipeline of the first heat exchanger, conveying the incinerated gas TO one end of a second hot-side pipeline of the second heat exchanger from the other end of the first hot-side pipeline of the first heat exchanger, and conveying the incinerated gas TO the outlet of the direct-fired incinerator (TO) from the other end of the second hot-side pipeline of the second heat exchanger; and
and (3) regulating and controlling a cold-side proportional air door: and a cold side proportion air door is arranged on the desorption concentrated gas pipeline, and the other end of the cold side proportion air door is used for allowing external air to enter so as to regulate and control the air volume of the desorption concentrated gas pipeline through the cold side proportion air door.
12. Energy efficient single runner cold side bypass over temperature control method according TO claim 8, 9, 10 or 11, characterized in that the outlet of the direct fired incinerator (TO) is further connected TO the chimney.
13. The energy efficient single wheel cold side bypass over temperature control method as claimed in claim 8, 9, 10 or 11 wherein said cooling air intake conduit is further for fresh air or outside air.
14. The energy-saving single-runner cold-side bypass over-temperature control method according to claim 8, 9, 10 or 11, wherein the exhaust gas inlet pipeline is further provided with an exhaust gas communication pipeline, the exhaust gas communication pipeline is connected with the cooling gas inlet pipeline, and the exhaust gas communication pipeline is further provided with an exhaust gas communication control valve to control the air volume of the exhaust gas communication pipeline.
15. The energy-saving single-runner cold-side bypass over-temperature control method as claimed in claim 8, 9, 10 or 11, wherein the desorption concentrated gas pipeline is further provided with a fan.
16. The energy-saving single-runner cold-side bypass over-temperature control method as claimed in claim 8, 9, 10 or 11, wherein the net gas discharge pipeline is further provided with a fan.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| TW109125791A TWI745007B (en) | 2020-07-30 | 2020-07-30 | Energy-saving single runner cold side passing temperature control system and method |
| TW109125791 | 2020-07-30 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN114060829A true CN114060829A (en) | 2022-02-18 |
Family
ID=79907914
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202010958034.7A Pending CN114060829A (en) | 2020-07-30 | 2020-09-14 | Energy-saving single-runner cold-side bypass over-temperature control system and method thereof |
Country Status (2)
| Country | Link |
|---|---|
| CN (1) | CN114060829A (en) |
| TW (1) | TWI745007B (en) |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP2223730B1 (en) * | 2007-09-12 | 2017-02-15 | Munters Corporation | Apparatus and method for in-situ high temperature regeneration of a rotor sorption concentrator |
| CN208779466U (en) * | 2018-08-20 | 2019-04-23 | 陕西宝昱科技工业有限公司 | A kind of direct-fired waste gas combustion furnace heating by the exhaust gases temperature-adjusting device |
| TWM576495U (en) * | 2018-11-30 | 2019-04-11 | 華懋科技股份有限公司 | Organic waste gas treatment and improvement system with highly efficient volatility |
| CN210544220U (en) * | 2019-06-14 | 2020-05-19 | 上海恒奕环境科技有限公司 | High-temperature activation system for waste gas treatment |
-
2020
- 2020-07-30 TW TW109125791A patent/TWI745007B/en active
- 2020-09-14 CN CN202010958034.7A patent/CN114060829A/en active Pending
Also Published As
| Publication number | Publication date |
|---|---|
| TW202204822A (en) | 2022-02-01 |
| TWI745007B (en) | 2021-11-01 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN112023620A (en) | High-temperature desorption method of volatile organic waste gas treatment system | |
| CN212481331U (en) | Energy-saving double-runner cold side bypass over-temperature control system | |
| CN212618367U (en) | Energy-saving double-runner high-concentration cold side bypass over-temperature control system | |
| CN114377516A (en) | Energy-saving type single-runner hot-side bypass over-temperature control system and method thereof | |
| CN214147937U (en) | Energy-saving single-runner high-concentration hot-side bypass over-temperature control system | |
| CN214345424U (en) | Energy-saving double-rotating-wheel high-concentration hot-side bypass over-temperature control system | |
| CN214261284U (en) | Energy-saving single-runner hot-side bypass over-temperature control system | |
| CN214275760U (en) | Energy-saving double-rotating-wheel hot-side bypass over-temperature control system | |
| TWI756748B (en) | Energy-saving dual-rotor cold side bypass temperature control system and method thereof | |
| CN113970109A (en) | Energy-saving double-rotating-wheel high-concentration cold-side bypass over-temperature control system and method thereof | |
| CN212481332U (en) | Energy-saving single-runner cold-side bypass over-temperature control system | |
| CN114060829A (en) | Energy-saving single-runner cold-side bypass over-temperature control system and method thereof | |
| CN214370247U (en) | Energy-saving single-runner high-concentration cold-side bypass over-temperature control system | |
| CN114383145A (en) | Energy-saving type single-runner high-concentration hot-side bypass over-temperature control system and method thereof | |
| CN114060830A (en) | Energy-saving single-runner high-concentration cold-side bypass over-temperature control system and method thereof | |
| CN114377515A (en) | Energy-saving double-rotating-wheel high-concentration hot-side bypass over-temperature control system and method thereof | |
| CN214513652U (en) | Energy-saving single-runner high-concentration hot bypass over-temperature control system | |
| CN214552355U (en) | Energy-saving double-runner high-concentration hot bypass over-temperature control system | |
| CN215085993U (en) | Double-rotating-wheel high-efficiency organic waste gas treatment system | |
| TWI823027B (en) | Energy-saving dual-runner hot side pass temperature control system and method thereof | |
| CN213019680U (en) | Volatile organic waste gas treatment system with double rotating wheels | |
| CN114588747A (en) | Double-rotating-wheel high-efficiency organic waste gas treatment system and method | |
| CN114588748A (en) | Double-rotary-wheel high-concentration organic waste gas treatment system and method | |
| CN115405937A (en) | Rotary wheel system with hot medium oil and method thereof | |
| CN115325550A (en) | Rotating wheel system with heat source 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 |