CN114383145B - Energy-saving single-rotor high-concentration heat side-bypass temperature control system and method thereof - Google Patents
Energy-saving single-rotor high-concentration heat side-bypass temperature control system and method thereof Download PDFInfo
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- CN114383145B CN114383145B CN202011435917.6A CN202011435917A CN114383145B CN 114383145 B CN114383145 B CN 114383145B CN 202011435917 A CN202011435917 A CN 202011435917A CN 114383145 B CN114383145 B CN 114383145B
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- 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
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- 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
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- 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
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- 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
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- 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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J11/00—Devices for conducting smoke or fumes, e.g. flues
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/40083—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption
- B01D2259/40088—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating
- B01D2259/4009—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating using hot gas
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Abstract
一种节能型单转轮高浓度热侧旁通过温控制系统及其方法，主要用于有机废气处理系统，且设有一直燃式焚烧炉，一第一热交换器、一第二热交换器、一第三热交换器、一第一冷侧输送管路、一第三冷侧输送管路、一吸附转轮及一烟囱，并通过在该直燃式焚烧炉的炉膛设有一热侧强排管路，且该热侧强排管路的另一端与该第三热交换器的第三热侧管路与该第二热交换器的第二热侧管路之间相连处、或与该第二热交换器的第二热侧管路与该第一热交换器的第一热侧管路之间相连处、或与该直燃式焚烧炉的出口之其中任一处连接；本发明能防止直燃式焚烧炉不会因炉温太高而发生过温的现象，甚至导致停机。
An energy-saving single-rotor high-concentration hot side bypass temperature control system and method thereof are mainly used in an organic waste gas treatment system and are provided with a direct-fired incinerator, a first heat exchanger, a second heat exchanger, a third heat exchanger, a first cold side delivery pipeline, a third cold side delivery pipeline, an adsorption rotor and a chimney, and a hot side forced exhaust pipeline is provided in the furnace of the direct-fired incinerator, and the other end of the hot side forced exhaust pipeline is connected to the third hot side pipeline of the third heat exchanger and the second hot side pipeline of the second heat exchanger, or to the second hot side pipeline of the second heat exchanger and the first hot side pipeline of the first heat exchanger, or to any one of the outlets of the direct-fired incinerator; the present invention can prevent the direct-fired incinerator from overheating due to too high a furnace temperature, or even cause shutdown.
Description
Technical Field
The invention relates TO an energy-saving single-runner high-concentration hot side bypass over-temperature control system and a method thereof, in particular TO an organic waste gas treatment system or similar equipment which can be used for adjusting the heat recovery amount or concentration when the concentration of Volatile Organic Compounds (VOCS) becomes high, so that the phenomenon that a direct-fired incinerator (TO) cannot be over-heated due TO too high furnace temperature or even stop is prevented when organic waste gas is treated, and is suitable for semiconductor industry, photoelectric industry or chemical related industry.
Background
At present, volatile organic gases (VOCs) are generated in the manufacturing and production processes of the semiconductor industry or the photoelectric industry, so that treatment equipment for treating the VOCs is installed in each factory area to avoid air pollution caused by direct discharge of the VOCs into the air. The concentrated gas desorbed by the treatment device is mostly delivered to the incinerator for combustion, and the combusted gas is delivered to a chimney for discharge.
However, in recent years, the relevant departments have very important views on air pollution, and therefore, the relevant atmospheric quality standards are defined on the emission standards of the chimney, and meanwhile, the relevant atmospheric quality standards are discussed in terms of the international regulatory trend.
Therefore, in view of the above-mentioned drawbacks, the present inventors have proposed an energy-saving single-wheel high-concentration hot side bypass overheat control system and method thereof for improving the efficiency of organic waste gas treatment, which can be easily assembled by a user, and which is a motivation for the present inventors to develop and develop the system.
Disclosure of Invention
The main objective of the present invention is TO provide an energy-saving single-runner high-concentration hot 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 third heat exchanger, a first cold side conveying pipeline, a third cold side conveying pipeline, an adsorption runner and a chimney, wherein a hot side forced-air discharge pipeline is arranged in a hearth of the direct-fired incinerator (TO), and the other end of the hot side forced-air discharge pipeline is connected with a position between a third hot side pipeline of the third heat exchanger and a second hot side pipeline of the second heat exchanger, or is connected with a position between a second hot side pipeline of the second heat exchanger and a first hot side pipeline of the first heat exchanger, or is connected with any position of outlets of the direct-fired incinerator (TO), so that when the concentration of Volatile Organic Compounds (VOCS) becomes high, the direct-fired incinerator (TO) can be regulated through the hot side forced-air discharge pipeline, and the heat recovery efficiency can not even be increased due TO the fact that the heat recovery efficiency of the direct-fired incinerator (TO) is high, and the heat recovery efficiency can not be caused when the whole heat recovery efficiency is increased.
Another object of the present invention is TO provide an energy-saving single-wheel high-concentration hot side bypass overtemperature control system and method thereof, wherein at least one damper is provided in the hot side forced air discharge pipeline, and the other end of the hot side forced air discharge pipeline is connected with the connection between the third hot side pipeline of the third heat exchanger and the second hot side pipeline of the second heat exchanger, or with the connection between the second hot side pipeline of the second heat exchanger and the first hot side pipeline of the first heat exchanger, or with any one of the outlets of the direct-fired incinerator (TO), so that when the concentration of Volatile Organic Compounds (VOCS) becomes high, the air quantity of the furnace chamber of the direct-fired incinerator (TO) can be adjusted through the hot side forced air discharge pipeline, and the partially incinerated high-temperature gas can be delivered TO the connection between the hot side pipelines of different heat exchangers, so that the hot side forced air discharge pipeline has the effect of adjusting the heat recovery quantity or concentration, and the phenomenon that the direct-fired incinerator (TO) cannot be excessively increased due TO the high temperature or even excessively high temperature during the treatment of the organic waste gas can be prevented.
For a further understanding of the nature, features, and aspects of the present invention, reference should be made to the following detailed description of the invention and to the accompanying drawings, which are provided by way of illustration only and not to limit the invention.
Drawings
Fig. 1 is a schematic diagram of a system architecture with hot side forced-induction piping according to a first embodiment of the present invention.
Fig. 2 is a schematic diagram of a system architecture with hot side forced-air piping according to a second embodiment of the present invention.
Fig. 3 is a schematic diagram of a system architecture with hot side forced-air piping according to a third embodiment of the present invention.
Fig. 4 is a flow chart of the main steps of the first embodiment of the present invention.
Fig. 5 is a flow chart of the main steps of a second embodiment of the present invention.
Fig. 6 is a flow chart of main steps of a third embodiment of the present invention.
Reference numerals illustrate:
10. direct-fired incinerator (TO) 101 and burner
102. Hearth 11, inlet
12. Outlet 20, first heat exchanger
21. First cold side pipe 22 and first hot side pipe
23. First cold side transfer line 30, second heat exchanger
31. Second cold side pipe 32, second hot side pipe
40. Third heat exchanger 41, third cold side line
42. Third hot side piping 43, third cold side conveying piping
60. Adsorption rotating wheel
601. Adsorption zone 602, cooling zone
603. Desorption zone 61 and exhaust gas inlet line
611. Exhaust gas communication pipeline 6111 and exhaust gas communication control valve
62. Purified gas discharge pipeline 621 and purified gas communication pipeline
6211. Clean air communication control valve 63 and cooling air inlet pipeline
64. Cooling gas delivery line 65, hot gas delivery line
66. Desorption concentrated gas pipeline 661, fan
80. Chimney
90. Hot side forced-ventilated line 901 and air damper
S100, inputting a gas S200 to be adsorbed, and inputting the gas to be adsorbed
S110, the adsorption runner adsorbs S210, and the adsorption runner adsorbs
S120, inputting cooling gas S220, inputting cooling gas
S130, conveying hot gas desorption S230 and conveying hot gas desorption
S140, desorption concentrated gas conveying S240 and desorption concentrated gas conveying
S150, incinerated gas conveying S250, incinerated gas conveying
S160, hot side strong exhaust pipeline adjustment S260, hot side strong exhaust pipeline adjustment
S300, inputting gas to be adsorbed
S310, adsorbing by an adsorption rotating wheel
S320, inputting cooling gas
S330, conveying hot gas for desorption
S340, desorption concentration gas delivery
S350, gas delivery after incineration
S360, hot side strong drain pipeline adjustment
Detailed Description
The present invention will be further described in detail below with reference to specific embodiments and with reference to the accompanying drawings, in order to make the objects, technical solutions and advantages of the present invention more apparent.
Referring TO fig. 1 TO 6, which are schematic diagrams of embodiments of the present invention, the best implementation of the energy-saving single-runner high-concentration hot side bypass overheat control system and the method thereof is applied TO a volatile organic waste gas treatment system or similar equipment in semiconductor industry, photoelectric industry or chemical related industry, mainly when the concentration of Volatile Organic Compounds (VOCS) becomes high, the system can have the effect of adjusting the heat recovery amount or concentration, so that the direct-fired incinerator (TO) can be prevented from being overheated due TO too high furnace temperature during the treatment of organic waste gas, and even the shutdown situation is caused.
The energy-saving single-runner high-concentration hot side bypass over-temperature control system of the present invention mainly comprises a direct-fired incinerator (TO) 10, a first heat exchanger 20, a second heat exchanger 30, a third heat exchanger 40, a first cold side conveying pipeline 23, a third cold side conveying pipeline 43, an adsorption runner 60 and a chimney 80 (as shown in fig. 1 TO 3), 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, and the third heat exchanger 40 is provided with a third cold side pipeline 41 and a third hot side pipeline 42. The direct-fired incinerator (TO) 10 is further provided with a furnace end 101 and a furnace chamber 102, the furnace end 101 is communicated with the furnace chamber 102, the first heat exchanger 20, the second heat exchanger 30 and the third heat exchanger 40 are respectively arranged in 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 3), the inlet 11 is arranged at the furnace end 101, the inlet 11 is connected with the other end of the third cold side pipeline 41 of the third heat exchanger 40, in addition, the outlet 12 is arranged at the furnace chamber 102, and the outlet 12 is connected with the chimney 80, so that the organic waste gas can enter the furnace end 101 from the inlet 11 for combustion, and then the combusted gas can pass through the furnace chamber 102 and be discharged from the outlet 12 TO the chimney 80 for emission, thereby having the energy saving effect.
The burner 101 of the direct-fired incinerator (TO) 10 can transfer the incinerated high-temperature gas TO one side of the third hot side pipeline 42 of the third heat exchanger 40 for heat exchange, transfer the incinerated high-temperature gas 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 third hot side pipeline 42 of the third heat exchanger 40, transfer the incinerated high-temperature gas TO one side of the first hot side pipeline 22 of the first heat exchanger 20 for heat exchange by the other side of the second hot side pipeline 32 of the second heat exchanger 30, and finally transfer the incinerated high-temperature gas TO the outlet 12 of the furnace 102 by the other side of the first hot side pipeline 22 of the first heat exchanger 20 (as shown in fig. 1 TO 3) and transfer the outlet 12 of the furnace 102 TO the chimney 80 for discharge through the chimney 80.
In addition, 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 with an exhaust gas inlet pipeline 61, a clean gas discharge pipeline 62, a cooling gas inlet pipeline 63, a cooling gas conveying pipeline 64, a hot gas conveying pipeline 65 and a desorption concentrated gas pipeline 66 (as shown in fig. 1 to 3). Wherein the adsorption rotor 60 is a zeolite concentration rotor or a concentration rotor of other materials.
Wherein one end of the exhaust gas inlet pipe 61 is connected to one side of the adsorption zone 601 of the adsorption wheel 60, so that the exhaust gas inlet pipe 61 can deliver organic exhaust gas to one side of the adsorption zone 601 of the adsorption wheel 60, and one end of the clean gas discharge pipe 62 is connected to the other side of the adsorption zone 601 of the adsorption wheel 60, the other end of the clean gas discharge pipe 62 is connected to the chimney 80, and the clean gas discharge pipe 62 is provided with a fan 621 (as shown in fig. 3), 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.
In addition, one side of the cooling zone 602 of the adsorption rotor 60 is connected to the cooling gas inlet pipe 63 to allow gas to enter the cooling zone 602 of the adsorption rotor 60 for cooling (as shown in fig. 1 to 3), while the other side of the cooling zone 602 of the adsorption rotor 60 is connected to one end of the cooling gas delivery pipe 64, 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 to deliver gas after 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 3), and furthermore, one end of the hot gas delivery pipe 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 pipe 65 is connected to the other end of the second cold side pipe 31 of the second heat exchanger 30 to enable high temperature hot gas heat exchanged via the second heat exchanger 30 to be delivered to the desorption zone 603 of the adsorption rotor 60 via the hot gas delivery pipe 65 for desorption.
The cooling zone 602 of the adsorption rotor 60 is provided with two embodiments, wherein in the first embodiment, the cooling air inlet pipe 63 connected to one side of the cooling zone 602 of the adsorption rotor 60 is used for introducing fresh air or external air (as shown in fig. 1), and the cooling of the cooling zone 602 of the adsorption rotor 60 is provided by the fresh air or external air. In the second embodiment, the exhaust gas inlet pipe 61 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 3), so that the exhaust gas in the exhaust gas inlet pipe 61 can be delivered to the cooling zone 602 of the adsorption rotor 60 through the exhaust gas communication pipe 611 for cooling, 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.
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 one end of the third cold side line 41 of the third heat exchanger 40 (as shown in fig. 1 to 3). In addition, the other end of the third cold side pipeline 41 of the third heat exchanger 40 is connected TO one end of the third cold side pipeline 43, while the other end of the third cold side pipeline 43 is connected TO the inlet 11 of the direct-fired incinerator (TO) 10, so that the desorbed concentrated gas desorbed at high temperature can be conveyed into one end of the first cold side pipeline 21 of the first heat exchanger 20 through the desorbed concentrated gas pipeline 66, and conveyed into one end of the first cold side pipeline 23 through the other end of the first cold side pipeline 21 of the first heat exchanger 20, and conveyed into one end of the third cold side pipeline 41 of the third heat exchanger 40 through the other end of the first cold side pipeline 23, and conveyed into one end of the third cold side pipeline 43 through the other end of the third cold side pipeline 41 of the third heat exchanger 40, and finally conveyed into the inlet 11 of the direct-fired incinerator (TO) 10 through the other end of the third cold side pipeline 43 (TO) (as shown in fig. 1 TO 3), so that the direct-fired incinerator (TO) can be incinerated by the high-temperature boiler (TO) TO reduce the volatile compounds 101. The desorption enriched gas line 66 is provided with a fan 661 to push and pull the desorption enriched gas into one end of the first cold side line 21 of the first heat exchanger 20.
In addition, the energy-saving single-runner high-concentration hot side bypass overtemperature control system of the present invention mainly has three embodiments, but the direct-fired incinerator (TO) 10, the first heat exchanger 20, the second heat exchanger 30, the third heat exchanger 40, the first cold side conveying pipeline 23, the third cold side conveying pipeline 43, the adsorption runner 60 and the chimney 80 in the three embodiments are designed in the same manner, and therefore, the contents of the direct-fired incinerator (TO) 10, the first heat exchanger 20, the second heat exchanger 30, the third heat exchanger 40, the first cold side conveying pipeline 23, the third cold side conveying pipeline 43, the adsorption runner 60 and the chimney 80 are not repeated, and the description is referred TO.
The difference between the first embodiment (as shown in fig. 1) is that the furnace 102 of the direct-fired incinerator (TO) 10 is provided with a hot side forced air duct 90, one end of the hot side forced air duct 90 is connected with the furnace 102 of the direct-fired incinerator (TO) 10, and the other end of the hot side forced air duct 90 is connected with the connection between the third hot side duct 42 of the third heat exchanger 40 and the second hot side duct 32 of the second heat exchanger 30, wherein the hot side forced air duct 90 is provided with at least one air damper 901, and two air dampers (not shown) can be provided in cooperation with the duct TO regulate the air quantity of the hot side forced air duct 90 through the air damper 901, so that when the concentration of the Volatile Organic Compounds (VOCS) becomes high, the air quantity of the furnace 102 of the direct-fired incinerator (TO) 10 can be regulated through the hot side forced air duct 90, and part of the burnt high-temperature gas is delivered TO the connection between the third hot side duct 42 of the third heat exchanger 40 and the second hot side duct 32 of the second heat exchanger 30, and the heat recovery phenomenon of the heat exchanger 10 can be prevented even when the concentration of the Volatile Organic Compounds (VOCS) becomes high, and the heat loss phenomenon of the incinerator is prevented from occurring at the heat recovery condition that the high temperature is caused by the heat concentration of the heat of the incinerator (TO) or the exhaust gas is too high, and the heat is not recovered.
The difference between the second embodiment (as shown in fig. 2) is that the furnace 102 of the direct-fired incinerator (TO) 10 is provided with a hot side forced air duct 90, one end of the hot side forced air duct 90 is connected with the furnace 102 of the direct-fired incinerator (TO) 10, and the other end of the hot side forced air duct 90 is connected with the connection between the second hot side duct 32 of the second heat exchanger 30 and the first hot side duct 22 of the first heat exchanger 20, wherein the hot side forced air duct 90 is provided with at least one damper 901, and two dampers (not shown) can be provided in cooperation with the duct TO regulate the air quantity of the hot side forced air duct 90 through the damper 901, so that when the concentration of the Volatile Organic Compounds (VOCS) becomes high, the air quantity of the furnace 102 of the direct-fired incinerator (TO) 10 can be regulated through the hot side forced air duct 90, and part of the burned high-temperature gas is delivered TO the connection between the second hot side duct 32 of the second heat exchanger 30 and the first hot side duct 22 of the first heat exchanger 20, and thus the heat recovery phenomenon of the direct-fired incinerator (TO) can be prevented even when the concentration of the Volatile Organic Compounds (VOCS) becomes high, and the heat recovery of the heat is not possible, and the heat is prevented from being too high, and the heat is caused by the heat of the heat-dissipating condition of the heat from the exhaust duct or the heat-up condition of the exhaust duct (TO be too high temperature and the heat-resistant condition or the exhaust gas (TO be too high).
The difference between the third embodiment (as shown in fig. 3) is that the furnace 102 of the direct-fired incinerator (TO) 10 is provided with a hot side forced-air duct 90, one end of the hot side forced-air duct 90 is connected with the furnace 102 of the direct-fired incinerator (TO) 10, and the other end of the hot side forced-air duct 90 is connected with the outlet 12 of the direct-fired incinerator (TO) 10, wherein the hot side forced-air duct 90 is provided with at least one air damper 901, and two air dampers (not shown) can be provided in cooperation with the duct, so that the air quantity of the hot side forced-air duct 90 can be regulated by the air damper 901, and therefore, when the concentration of Volatile Organic Compounds (VOCS) becomes high, the air quantity of the furnace 102 of the direct-fired incinerator (TO) 10 can be regulated by the hot side forced-air duct 90, and part of the burnt high-temperature gas can be delivered TO the outlet 12 of the direct-fired incinerator (TO) 10, so that the hot side forced-air duct 90 has the effect of regulating the heat quantity or concentration, and the situation that the waste gas of the direct-fired incinerator (TO) cannot even stop due TO the high temperature condition is prevented when the waste gas is caused by the treatment of the high temperature of the direct-fired incinerator (TO).
The energy-saving single-wheel high-concentration hot side bypass over-temperature control method of the present invention is mainly used in an organic waste gas treatment system, and comprises a direct-fired incinerator (TO) 10, a first heat exchanger 20, a second heat exchanger 30, a third heat exchanger 40, a first cold side conveying pipeline 23, a third cold side conveying pipeline 43, an adsorption wheel 60 and a chimney 80 (as shown in fig. 1 TO 3), 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, the third heat exchanger 40 is provided with a third cold side pipeline 41 and a third hot side pipeline 42, one end of the first cold side conveying pipeline 23 is connected with the other end of the first cold side pipeline 21, the other end of the first cold side conveying pipeline 23 is connected with one end of the third cold side pipeline 41, one end of the third cold side conveying pipeline 43 is connected with the other end of the third cold side pipeline 41, and the other end of the third cold side conveying pipeline 43 is connected with the TO the direct-fired inlet (TO) of the direct-fired incinerator (10). The direct-fired incinerator (TO) 10 is provided with a furnace end 101 and a furnace chamber 102, the furnace end 101 is communicated with the furnace chamber 102, the first heat exchanger 20, the second heat exchanger 30 and the third heat exchanger 40 are respectively arranged in 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 3), the inlet 11 is arranged at the furnace end 101, the inlet 11 is connected with the other end of the third cold side pipeline 41 of the third heat exchanger 40, in addition, the outlet 12 is arranged at the furnace chamber 102, and the outlet 12 is connected with the chimney 80, so that the organic waste gas can enter the furnace end 101 from the inlet 11 for combustion, and the combusted gas can pass through the furnace chamber 102 and be discharged from the outlet 12 TO the chimney 80 for discharge, thereby having the energy-saving effect.
The burner 101 of the direct-fired incinerator (TO) 10 can transfer the incinerated high-temperature gas TO one side of the third hot side pipeline 42 of the third heat exchanger 40 for heat exchange, transfer the incinerated high-temperature gas 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 third hot side pipeline 42 of the third heat exchanger 40, transfer the incinerated high-temperature gas TO one side of the first hot side pipeline 22 of the first heat exchanger 20 for heat exchange by the other side of the second hot side pipeline 32 of the second heat exchanger 30, and finally transfer the incinerated high-temperature gas TO the outlet 12 of the furnace 102 by the other side of the first hot side pipeline 22 of the first heat exchanger 20 (as shown in fig. 1 TO 3) and transfer the outlet 12 of the furnace 102 TO the chimney 80 for discharge through the chimney 80.
In addition, 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 with an exhaust gas inlet pipeline 61, a clean gas discharge pipeline 62, a cooling gas inlet pipeline 63, a cooling gas delivery pipeline 64, a hot gas delivery pipeline 65 and a desorption concentrated gas pipeline 66 (as shown in fig. 1 to 3). Wherein the adsorption rotor 60 is a zeolite concentration rotor or a concentration rotor of other materials.
The main steps of the control method (as shown in fig. 4) include inputting the gas to be adsorbed in step S100, and feeding the exhaust gas into one side of the adsorption zone 601 of the adsorption wheel 60 through the other end of the exhaust gas inlet pipe 61. And the next step S110 is performed after the above step S100 is completed.
The next step S110 is to adsorb the gas by the adsorption zone 601 of the adsorption wheel 60, and then to output the adsorbed gas from the other side of the adsorption zone 601 of the adsorption wheel 60 through the other end of the clean gas discharge line 62. And the next step S120 is performed after the above step S110 is completed.
The other side of the adsorption zone 601 of the adsorption wheel 60 in the above step S110 is connected to the clean air discharge pipe 62 to connect with the chimney 80 through the other end of the clean air discharge pipe 62, and the clean air discharge pipe 62 is provided with a fan 621 (as shown in fig. 3), so that the adsorbed gas in the clean air discharge pipe 62 can be pushed into the chimney 80 by the fan 621 for discharge.
The next step S120 is to supply cooling gas to the cooling zone 602 of the adsorption rotor 60 through the other end of the cooling gas supply line 63, and then to supply cooling gas passing through the cooling zone 602 of the adsorption rotor 60 to one end of the second cold side line 31 of the second heat exchanger 30 through the other end of the cooling gas supply line 64. And the next step S130 is performed after the above step S120 is completed.
The cooling zone 602 of the adsorption rotor 60 in the above step S120 is provided with two embodiments, wherein the first embodiment is that the cooling air inlet pipe 63 connected to one side of the cooling zone 602 of the adsorption rotor 60 is used for introducing fresh air or external air (as shown in fig. 1), and the cooling of the cooling zone 602 of the adsorption rotor 60 is provided by the fresh air or external air. In the second embodiment, the exhaust gas inlet pipe 61 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 3), so that the exhaust gas in the exhaust gas inlet pipe 61 can be delivered to the cooling area 602 of the adsorption 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 to control the air volume of the exhaust gas communication pipe 611.
The next step S130 is to carry out the desorption of the hot gas by feeding the hot gas to the desorption region 603 of the adsorption rotor 60 through the hot gas feeding line 65 connected to the other end of the second cold side line 31 of the second heat exchanger 30 and feeding the desorbed enriched gas to the one end of the first cold side line 21 of the first heat exchanger 20 through the other end of the desorbed enriched gas line 66. And the next step S140 is performed after the above step S130 is completed.
The desorption concentrated gas line 66 in the above step S130 is provided with a fan 661 (as shown in fig. 3) to push and pull the desorption concentrated gas into the first cold side line 21 of the first heat exchanger 20.
The next step S140 is TO desorb the concentrated gas, which is then transferred TO one end of the third cold side pipe 41 of the third heat exchanger 40 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, and transferred TO the inlet 11 of the direct combustion incinerator (TO) 10 through the third cold side transfer pipe 43 connected TO the other end of the third cold side pipe 41 of the third heat exchanger 40. After the step S140 is completed, the next step S150 is performed.
The next step S150 is TO transfer the burned gas generated by burning the burner 101 of the direct-fired incinerator (TO) 10 TO one end of the third hot side pipe 42 of the third heat exchanger 40, TO one end of the second hot side pipe 32 of the second heat exchanger 30 from the other end of the third hot side pipe 42 of the third heat exchanger 40, 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 finally TO the outlet 12 of the direct-fired incinerator (TO) 10 from the other end of the first hot side pipe 22 of the first heat exchanger 20. And the next step S160 is performed after the completion of the above step S150.
The next step is TO perform hot side forced air duct adjustment in step S160, wherein the furnace 102 of the direct-fired incinerator (TO) 10 is provided with a hot side forced air duct 90, one end of the hot side forced air duct 90 is connected TO the furnace 102 of the direct-fired incinerator (TO) 10, the other end of the hot side forced air duct 90 is connected TO the connection between the third hot side duct 42 of the third heat exchanger 40 and the second hot side duct 32 of the second heat exchanger 30, and the hot side forced air duct 90 is provided with at least one damper 901 TO adjust the air volume of the furnace 102 of the direct-fired incinerator (TO) 10 through the hot side forced air duct 90.
Wherein in the step S160, one end of the hot side forced-air pipe 90 is connected TO the furnace 102 of the direct-fired incinerator (TO) 10, and the other end of the hot side forced-air pipe 90 is connected TO the connection between the third hot side pipe 42 of the third heat exchanger 40 and the second hot side pipe 32 of the second heat exchanger 30, wherein the hot side forced-air pipe 90 is provided with at least one damper 901, and two dampers (not shown) may be provided in combination with the hot side forced-air pipe 90 TO regulate the air volume of the hot side forced-air pipe 90 through the damper 901, so that when the concentration of the Volatile Organic Compound (VOCS) becomes high, the air volume of the furnace 102 of the direct-fired incinerator (TO) 10 can be regulated through the hot side forced-air pipe 90, and part of the incinerated high-temperature gas is delivered TO the connection between the third hot side pipe 42 of the third heat exchanger 40 and the second hot side pipe 32 of the second heat exchanger 30, so that the hot side forced-air pipe 90 has the heat quantity regulation or the concentration of the hot side forced-air pipe 90 can be regulated, and thus the heat recovery of the direct-fired incinerator (TO) can be prevented from being stopped even if the concentration of the Volatile Organic Compound (VOCS) becomes high, and the waste gas is not likely TO cause TO be too high.
In addition, the energy-saving single-runner high-concentration hot side bypass overtemperature control method of the present invention mainly has three implementation forms, but in the first implementation form (as shown in fig. 4), the gas to be adsorbed is input in step S100, the adsorption runner is adsorbed in step S110, the cooling gas is input in step S120, the hot gas is delivered and desorbed in step S130, the concentrated gas is delivered in step S140, the burnt gas is delivered in step S150, and the hot side strong exhaust pipe is regulated in step S160, so that the description is given above, and the description is referred to above.
The same design as the step S100 input to the gas to be adsorbed, the step S110 adsorption wheel input to the adsorption, the step S120 input to the cooling gas, the step S130 input to the cooling gas, the step S240 desorption concentration gas and the step S250 incineration gas transmission in the second embodiment (shown in fig. 5) is adopted for the step S200 input to the gas to be adsorbed, the step S310 adsorption wheel input to the adsorption, the step S320 input to the cooling gas, the step S330 input to the hot gas desorption, the step S340 desorption concentration gas and the step S350 incineration gas transmission in the third embodiment (shown in fig. 6), and the difference is only the content of the strong exhaust pipe adjustment in the hot side of the step S160.
Therefore, the same contents as the gas to be adsorbed in step S100, the adsorption wheel in step S110, the cooling gas in step S120, the hot gas desorption in step S130, the desorption concentrated gas in step S140, and the gas transfer after incineration in step S150 are not repeated, and reference is made to the above description. The hot side strong drain adjustment of step S260 in the second embodiment (shown in fig. 5) and the hot side strong drain adjustment of step S360 in the third embodiment (shown in fig. 6) will be described below.
The difference between the second embodiment (as shown in fig. 5) is that the hot side forced-air line adjustment in step S260 is that the furnace 102 of the direct-fired incinerator (TO) 10 is provided with a hot side forced-air line 90, one end of the hot side forced-air line 90 is connected with the furnace 102 of the direct-fired incinerator (TO) 10, the other end of the hot side forced-air line 90 is connected with the connection between the second hot side line 32 of the second heat exchanger 30 and the first hot side line 22 of the first heat exchanger 20, and the hot side forced-air line 90 is provided with at least one damper 901 for adjusting the air volume of the furnace 102 of the direct-fired incinerator (TO) 10 through the hot side forced-air line 90.
In the step S260, one end of the hot side forced air pipe 90 is connected TO the furnace 102 of the direct-fired incinerator (TO) 10, while the other end of the hot side forced air pipe 90 is connected TO the connection between the second hot side pipe 32 of the second heat exchanger 30 and the first hot side pipe 22 of the first heat exchanger 20, wherein the hot side forced air pipe 90 is provided with at least one damper 901, and two dampers (not shown) may be provided in combination with the hot side forced air pipe 90 TO regulate the air volume of the hot side forced air pipe 90 through the damper 901, so that when the concentration of Volatile Organic Compounds (VOCS) becomes high, the air volume of the furnace 102 of the direct-fired incinerator (TO) 10 can be regulated through the hot side forced air pipe 90, and part of the incinerated high-temperature gas is delivered TO the connection between the second hot side pipe 32 of the second heat exchanger 30 and the first hot side pipe 22 of the first heat exchanger 20, so that the hot side forced air pipe 90 has the effect of regulating the heat quantity or the concentration, and thus the direct-fired incinerator (TO) can be prevented from being stopped even if the concentration of Volatile Organic Compounds (VOCS) becomes high, and the waste gas is not likely TO cause the heat recovery phenomenon of the direct-fired incinerator (TO occur.
The difference in the third embodiment (as shown in fig. 6) is that the hot side forced-air line adjustment in step S360 is that the furnace 102 of the direct-fired incinerator (TO) 10 is provided with a hot side forced-air line 90, one end of the hot side forced-air line 90 is connected with the furnace 102 of the direct-fired incinerator (TO) 10, the other end of the hot side forced-air line 90 is connected with the outlet 12 of the direct-fired incinerator (TO) 10, and the hot side forced-air line 90 is provided with at least one damper 901 TO adjust the air volume of the furnace 102 of the direct-fired incinerator (TO) 10 through the hot side forced-air line 90.
In the step S360, one end of the hot side forced-air pipe 90 is connected TO the furnace 102 of the direct-fired incinerator (TO) 10, and the other end of the hot side forced-air pipe 90 is connected TO the outlet 12 of the direct-fired incinerator (TO) 10, wherein the hot side forced-air pipe 90 is provided with at least one damper 901, and two dampers (not shown) may be provided in cooperation with the hot side forced-air pipe 90, so that the air volume of the hot side forced-air pipe 90 is regulated by the damper 901, and thus, when the concentration of the Volatile Organic Compound (VOCS) becomes high, the air volume of the furnace 102 of the direct-fired incinerator (TO) 10 can be regulated by the hot side forced-air pipe 90, and the partially incinerated high-temperature gas can be delivered TO the outlet 12 of the direct-fired incinerator (TO) 10, so that the hot side forced-air pipe 90 has the effect of regulating the heat recovery amount or concentration, and the phenomenon that the direct-fired incinerator (TO) 10 cannot be stopped due TO too high furnace temperature or even caused by too high temperature during the treatment of the organic waste gas can be prevented.
From the foregoing detailed description, it will be apparent to those skilled in the art that the present invention can be achieved in practice in accordance with the principles of the patent statutes.
The foregoing description of the embodiments has been provided for the purpose of illustrating the general principles of the invention, and is not meant to limit the invention thereto, but to limit the invention thereto, and any modifications, equivalents, improvements and equivalents thereof may be made without departing from the spirit and principles of the invention.
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| TW109136203A TWI826736B (en) | 2020-10-20 | 2020-10-20 | Energy-saving single-runner high-concentration hot side pass temperature control system and method thereof |
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