CN114377515A

CN114377515A - Energy-saving double-rotating-wheel high-concentration hot-side bypass over-temperature control system and method thereof

Info

Publication number: CN114377515A
Application number: CN202011386304.8A
Authority: CN
Inventors: 郑石治; 林国源; 扶亚民; 陈宗贤; 刘邦昱
Original assignee: Shanghai Huamao Environmental Protection Energy Saving Equipment Co ltd; Desiccant Technology Corp
Current assignee: Shanghai Huamao Environmental Protection Energy Saving Equipment Co ltd; Desiccant Technology Corp
Priority date: 2020-10-16
Filing date: 2020-12-02
Publication date: 2022-04-22
Also published as: TWI788715B; TW202217193A

Abstract

The invention relates to an energy-saving double-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, a first heat exchanger, a second heat exchanger, a third heat exchanger, a fourth heat exchanger, a first cold-side conveying pipeline, a fourth cold-side conveying pipeline, a first adsorption runner, a second adsorption runner and a chimney, wherein a hot-side forced exhaust pipeline is arranged in a hearth of the direct-fired incinerator, and the other end of the hot-side forced exhaust pipeline is connected with a joint between a fourth hot-side pipeline of the fourth heat exchanger and a third hot-side pipeline of the third heat exchanger, or is connected with a joint 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 joint between a second hot-side pipeline of the second heat exchanger and a first hot-side pipeline of the first heat exchanger, Or to any of the outlets of the direct-fired incinerator.

Description

Energy-saving double-rotating-wheel high-concentration hot-side bypass over-temperature control system and method thereof

Technical Field

The invention relates TO an energy-saving double-runner high-concentration hot-side bypass over-temperature control system and a method thereof, in particular TO an energy-saving double-runner high-concentration hot-side bypass over-temperature control system and a method thereof, which have the effect of adjusting the heat recovery amount or the concentration when the concentration of Volatile Organic Compounds (VOCs) is higher, so that a direct-fired incinerator (TO) can be prevented from generating over-temperature phenomenon caused by too high incinerator temperature and even stopping the incinerator when organic waste gas is treated, and the energy-saving double-runner high-concentration hot-side bypass over-temperature control system is suitable for organic waste gas treatment systems or similar equipment in the semiconductor industry, the photoelectric industry or the chemical related 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 delivered to the incinerator for combustion, and the combusted gas is delivered to a chimney for emission.

However, in recent years, air pollution is very important to central governments or governments of various places, and therefore, relevant air quality standards are established on emission standards of chimneys, and meanwhile, the air pollution is developed according to international regulation trends and is examined on a periodic basis.

Therefore, in view of the above-mentioned shortcomings, it is an object of the present invention to provide an energy-saving dual-rotor high-concentration hot-side bypass over-temperature control system and method thereof capable of improving the organic waste gas treatment efficiency, which can be easily operated and assembled by a user.

Disclosure of Invention

The invention mainly aims TO provide an energy-saving type double-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 fourth heat exchanger, a first cold-side conveying pipeline, a fourth cold-side conveying pipeline, a first adsorption rotating wheel, a second adsorption rotating wheel and a chimney, wherein a hot-side forced exhaust pipeline is arranged in a hearth of the direct-fired incinerator (TO), and the other end of the hot-side forced exhaust pipeline is connected with a position between the fourth hot-side pipeline of the fourth heat exchanger and the third pipeline of the third heat exchanger, or is connected with a position between the third hot-side pipeline of the third heat exchanger and the second pipeline of the second heat exchanger, or is connected with a position between the second hot-side pipeline of the second heat exchanger and the first hot-side pipeline of the first heat exchanger, Or any one of the outlets of the direct-fired incinerator (TO), thereby, when the concentration of the Volatile Organic Compounds (VOCs) is increased, the air quantity of the hearth of the direct-fired incinerator (TO) can be adjusted through the hot side forced exhaust pipeline, so that the heat recovery quantity or the concentration can be adjusted, and the direct-fired incinerator (TO) can be prevented from generating an over-temperature phenomenon caused by too high incinerator temperature and even causing the shutdown when organic waste gas is treated, thereby increasing the overall practicability.

The invention also provides an energy-saving double-runner high-concentration hot-side bypass over-temperature control system and a method thereof, wherein at least one damper is arranged on a hot-side forced exhaust pipeline, the other end of the hot-side forced exhaust pipeline is connected with a joint between a fourth hot-side pipeline of a fourth heat exchanger and a third hot-side pipeline of a third heat exchanger, or is connected with a joint 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 joint 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 one of outlets of the direct-fired incinerators (TO), so that when the concentration of Volatile Organic Compounds (VOCs) is high, the air volume of a hearth of the direct-fired incinerator (TO) can be adjusted through the hot-side forced exhaust pipeline, and partially-fired high-temperature gas is conveyed TO the joints of the hot-side pipelines of different heat exchangers, the hot side forced exhaust pipeline has the efficiency of adjusting the heat recovery amount or concentration, so that when organic waste gas is treated, 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 the whole usability is further improved.

For a better understanding of the nature, features and aspects of the present invention, reference should be made to the following detailed description of the invention, taken in conjunction with the accompanying drawings, which are provided for purposes of illustration and description only and are not intended to be limiting.

Drawings

FIG. 1 is a schematic diagram of a system architecture with a hot-side forced-exhaust pipeline according to a first embodiment of the present invention;

FIG. 2 is a schematic diagram of a system architecture with a hot-side forced-exhaust pipeline according to a second embodiment of the present invention;

FIG. 3 is a schematic diagram of a system having a hot-side forced-exhaust pipeline according to a third embodiment of the present invention;

FIG. 4 is a schematic diagram of a system architecture with a hot-side forced-exhaust pipeline according to a fourth embodiment of 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 a 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.

Description of the symbols:

10. direct-fired incinerator (TO) 101, furnace end

102. Hearth 11, entrance

12. Outlet 20, first Heat exchanger

21. A first cold side pipeline 22 and a first hot side pipeline

23. First cold-side transfer line 30, second heat exchanger

31. A second cold side duct 32, a second hot side duct

40. Third heat exchanger 41, third cold-side line

42. Third hot side pipeline 50 and fourth heat exchanger

51. A fourth cold side duct 52, a fourth hot side duct

53. Fourth cold-side transfer line 60, first adsorption rotor

601. Adsorption zone 602, cooling zone

603. Desorption zone 61, exhaust gas inlet line

611. Waste gas communicating pipeline 6111 and waste gas communicating control valve

62. The first purified gas discharge pipeline 621 and the first purified gas communication pipeline

6211. First clean gas communication control valve 63 and first cooling gas inlet pipeline

64. A first cooling gas delivery line 65, a first hot gas delivery line

66. First desorption concentrated gas pipeline 661, fan

70. Second adsorption rotating wheel 701 and adsorption zone

702. Cooling zone 703, desorption zone

71. Second purified gas discharge pipeline 711 and fan

72. Second cooling air inlet pipeline 73 and second cooling air delivery pipeline

74. Second hot gas conveying pipeline 75 and second desorption concentrated gas pipeline

751. Fan 80 and chimney

90. Hot side forced exhaust pipeline 901 and air damper

S100, inputting gas to be adsorbed S200, and inputting gas to be adsorbed

S110, adsorption of the first adsorption rotating wheel S210 and adsorption of the first adsorption rotating wheel

S120, inputting a first cooling gas S220, and inputting the first cooling gas

S130, conveying first hot gas for desorption S230 and conveying first hot gas for desorption

S140, conveying the desorbed concentrated gas S240 and conveying the desorbed concentrated gas

S150, burned gas transportation S250, and burned gas transportation

S160, adsorbing by the second adsorption rotating wheel S260 and adsorbing by the second adsorption rotating wheel

S170, inputting a second cooling gas S270 and inputting the second cooling gas

S180, conveying second hot gas for desorption S280 and conveying second hot gas for desorption

S190, adjusting S290 of hot side forced exhaust pipeline and adjusting of hot side forced exhaust pipeline

S300, inputting gas to be adsorbed S400, and inputting gas to be adsorbed

S310, adsorption of the first adsorption rotating wheel S410 and adsorption of the first adsorption rotating wheel

S320, inputting a first cooling gas S420, and inputting the first cooling gas

S330, conveying a first hot gas for desorption S430 and conveying a first hot gas for desorption

S340, conveying the desorption concentrated gas S440 and conveying the desorption concentrated gas

S350, burned gas delivery S450, and burned gas delivery

S360, adsorbing by the second adsorption rotating wheel S460 and adsorbing by the second adsorption rotating wheel

S370, inputting second cooling gas S470, and inputting second cooling gas

S380, conveying second hot gas for desorption S480 and conveying second hot gas for desorption

S390, adjusting the hot side forced exhaust pipeline S490 and adjusting the hot side forced exhaust pipeline

Detailed Description

Referring TO fig. 1 TO 8, schematic diagrams of embodiments of the present invention are shown, and a preferred embodiment of the energy-saving dual-rotor high-concentration hot-side bypass over-temperature control system and method thereof of the present invention is applied TO a volatile organic waste gas treatment system or the like in the semiconductor industry, the photoelectric industry or the chemical industry, mainly when the concentration of Volatile Organic Compounds (VOCs) becomes high, the system can have an effect of adjusting the heat recovery amount or concentration, so that the organic waste gas can be treated without over-temperature of a direct-fired incinerator (TO) caused by too high furnace temperature, even shutdown.

The energy-saving dual-runner high-concentration hot-side bypass over-temperature control system of the present invention mainly includes a combination design of a direct-fired incinerator (TO)10, a first heat exchanger 20, a second heat exchanger 30, a third heat exchanger 40, a fourth heat exchanger 50, a first cold-side conveying pipeline 23, a fourth cold-side conveying pipeline 53, a first adsorption runner 60, a second adsorption runner 70 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, the third heat exchanger 40 is provided with a third cold-side pipeline 41 and a third hot-side pipeline 42, and the fourth heat exchanger 50 is provided with a fourth cold-side pipeline 51 and a fourth hot-side pipeline 52. The direct-fired incinerator (TO)10 is provided with a burner 101 and a furnace chamber 102, the furnace end 101 is communicated with the furnace chamber 102, and the first heat exchanger 20, the second heat exchanger 30, the third heat exchanger 40 and the fourth heat exchanger 50 are respectively arranged in the direct-fired incinerator (TO)10, and the direct combustion incinerator (TO)10 is provided with an inlet 11 and an outlet 12 (as shown in fig. 1 TO 4), and the inlet 11 is provided at the burner 101, and the inlet 11 is connected to the other end of the fourth cold-side pipe 51 of the fourth heat exchanger 50, and, furthermore, the outlet 12 is disposed at the furnace 102, and the outlet 12 is connected to 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 102 and be discharged from the outlet 12 to the chimney 80 for discharge, thereby saving energy.

The burner 101 of the direct combustion type incinerator (TO)10 can firstly deliver the burned high-temperature gas TO one side of the fourth hot-side pipeline 52 of the fourth heat exchanger 50 for heat exchange, and the burned high-temperature gas is then delivered TO one side of the third hot-side pipeline 42 of the third heat exchanger 40 by the other side of the fourth hot-side pipeline 52 of the fourth heat exchanger 50 for heat exchange, and the burned 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 third hot-side pipeline 42 of the third heat exchanger 40, and then the burned high-temperature gas is then delivered 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 for heat exchange, and finally the burned high-temperature gas is delivered TO the outlet 12 of the furnace chamber 102 by the other side of the first hot-side pipeline 22 of the first heat exchanger 20 (see fig. 1) To fig. 4) and then conveyed by the outlet 12 of the furnace 102 to the stack 80 for discharge through the stack 80.

In addition, the first adsorption rotor 60 of the present invention is provided with an adsorption region 601, a cooling region 602 and a desorption region 603, the first adsorption rotor 60 is connected with a waste gas inlet line 61, a first purified gas discharge line 62, a first cooling gas inlet line 63, a first cooling gas delivery line 64, a first hot gas delivery line 65 and a first desorption concentrated gas line 66 (as shown in fig. 1 to 4), the second adsorption rotor 70 is provided with an adsorption region 701, a cooling region 702 and a desorption region 703, and the second adsorption rotor 70 is connected with a second purified gas discharge line 71, a second cooling gas inlet line 72, a second cooling gas delivery line 73, a second hot gas delivery line 74 and a second desorption concentrated gas line 75. Wherein the first adsorption rotor 60 and the second adsorption rotor 70 are zeolite concentration rotors or other material concentration rotors, respectively.

One end of the exhaust gas inlet pipeline 61 is connected to one side of the adsorption region 601 of the first adsorption rotor 60, so that the exhaust gas inlet pipeline 61 can deliver the organic exhaust gas to one side of the adsorption region 601 of the first adsorption rotor 60, one end of the first purge gas exhaust pipeline 62 is connected to the other side of the adsorption region 601 of the first adsorption rotor 60, and one end of the first purge gas exhaust pipeline 62 is connected to one side of the adsorption region 701 of the second adsorption rotor 70, so that the organic exhaust gas can be delivered into the adsorption region 701 of the second adsorption rotor 70 through the first purge gas exhaust pipeline 62 after adsorbing organic matters through the adsorption region 601 of the first adsorption rotor 60 (as shown in fig. 1 to 4). The other side of the adsorption region 701 of the second adsorption rotor 70 is connected to the second purified gas discharge pipe 71, so as to be connected to the chimney 80 through the other end of the second purified gas discharge pipe 71, and the second purified gas discharge pipe 71 is provided with a fan 711 (as shown in fig. 3 and 4), so that the fan 711 can push and pull the adsorbed gas in the second purified gas discharge pipe 71 into the chimney 80 for discharge.

In addition, one side of the cooling region 602 of the first adsorption rotor 60 is connected to the first cooling gas inlet pipe 63, so that the gas enters the cooling region 602 of the first adsorption rotor 60 for cooling (as shown in fig. 1 to 4), the other side of the cooling region 602 of the first adsorption rotor 60 is connected to one end of the first cooling gas conveying pipe 64, the other end of the first cooling gas conveying pipe 64 is connected to one end of the third cold side pipe 41 of the third heat exchanger 40, so that the gas after entering the cooling region 602 of the first adsorption rotor 60 is conveyed into the third heat exchanger 40 for heat exchange (as shown in fig. 1 to 4), furthermore, one end of the first hot gas conveying pipe 65 is connected to the other side of the desorption region 603 of the first adsorption rotor 60, and the other end of the first hot gas conveying pipe 65 is connected to the other end of the third cold side pipe 41 of the third heat exchanger 40, the high-temperature hot gas heat-exchanged by the third heat exchanger 40 can be transferred to the desorption region 603 of the first adsorption rotor 60 through the first hot gas transfer line 65 for desorption.

The cooling area 602 of the first sorption rotor 60 has two embodiments, wherein the first embodiment is that the first cooling air inlet pipe 63 connected to one side of the cooling area 602 of the first sorption rotor 60 is used for introducing fresh air or external air (as shown in fig. 1), and the cooling area 602 of the first sorption rotor 60 is provided by the fresh air or the external air. In another 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 first cooling gas inlet pipe 63 (as shown in fig. 3) so as to convey the exhaust gas in the exhaust gas inlet pipe 61 to the cooling zone 602 of the first 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 for controlling the air volume of the exhaust gas communication pipe 611.

In addition, one side of the cooling region 702 of the second adsorption rotor 70 is connected to the second cooling gas inlet pipe 72, so that the gas enters the cooling region 702 of the second adsorption rotor 70 for cooling (as shown in fig. 1 to 4), the other side of the cooling region 702 of the second adsorption rotor 70 is connected to one end of the second cooling gas conveying pipe 73, the other end of the second cooling gas conveying pipe 73 is connected to one end of the second cold-side pipe 31 of the second heat exchanger 30, so that the gas entering the cooling region 702 of the second adsorption rotor 70 is conveyed into the second heat exchanger 30 for heat exchange (as shown in fig. 1 to 4), furthermore, one end of the second hot gas conveying pipe 74 is connected to the other side of the desorption region 703 of the second adsorption rotor 70, and the other end of the second hot gas conveying pipe 74 is connected to the other end of the second cold-side pipe 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 703 of the second adsorption rotor 70 through the second hot gas transfer line 74 for desorption.

The cooling zone 702 of the second sorption rotor 70 has two embodiments, wherein the first embodiment is that the second cooling air inlet pipe 72 connected to one side of the cooling zone 702 of the second sorption rotor 70 is used for introducing fresh air or external air (as shown in fig. 1), and the cooling zone 702 of the second sorption rotor 70 is cooled by the fresh air or the external air. In another second embodiment, the first net gas discharging pipeline 62 is provided with a first net gas communicating pipeline 621, and the other end of the first net gas communicating pipeline 621 is connected to the second cooling gas inlet pipeline 72 (as shown in fig. 3 and fig. 4) so as to convey the gas in the first net gas discharging pipeline 62 to the cooling zone 702 of the second adsorption rotating wheel 70 for cooling through the first net gas communicating pipeline 621, and the first net gas communicating pipeline 621 is provided with a first net gas communicating control valve 6211 so as to control the air volume of the first net gas communicating pipeline 621.

In addition, one end of the first desorption concentrated gas pipeline 66 is connected to one side of the desorption region 603 of the first adsorption rotor 60, and the other end of the first desorption concentrated gas pipeline 66 is connected to one end of the first cold-side pipeline 21 of the first heat exchanger 20, wherein the other end of the first cold-side pipeline 21 of the first heat exchanger 20 is connected to one end of the first cold-side conveying pipeline 23, and the other end of the first cold-side conveying pipeline 23 is connected to one end of the fourth cold-side pipeline 51 of the fourth heat exchanger 50 (as shown in fig. 1 to 4). Furthermore, the other end of the fourth cold-side pipe 51 of the fourth heat exchanger 50 is connected TO one end of the fourth cold-side transfer pipe 53, and the other end of the fourth cold-side transfer pipe 53 is connected TO the inlet 11 of the direct-fired 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 pipe 21 of the first heat exchanger 20 through the first desorption-concentrated gas pipe 66, and transferred into one end of the first cold-side transfer pipe 23 through the other end of the first cold-side pipe 21 of the first heat exchanger 20, and transferred into one end of the fourth cold-side pipe 51 of the fourth heat exchanger 50 through the other end of the first cold-side transfer pipe 23, and then transferred into one end of the fourth cold-side transfer pipe 53 through the other end of the fourth cold-side pipe 51 of the fourth heat exchanger 50, finally, the other end of the fourth cold-side conveying pipe 53 is conveyed into the inlet 11 of the direct-fired incinerator (TO)10 (as shown in FIGS. 1 TO 4), so that the furnace head 101 of the direct-fired incinerator (TO)10 can be pyrolyzed TO reduce volatile organic compounds. The first desorption/condensation gas pipe 66 is further provided with a fan 661 for pushing and pulling the desorption/condensation gas into one end of the first cold-side pipe 21 of the first heat exchanger 20.

In addition, one end of the second concentrated desorption gas pipeline 75 is connected to one side of the desorption region 703 of the second adsorption rotor 70, wherein there are two embodiments for the other end of the second concentrated desorption gas pipeline 75, and the first embodiment is that the other end of the second concentrated desorption gas pipeline 75 is connected to the exhaust gas inlet pipeline 61 (as shown in fig. 1 and 3), so that the concentrated gas can enter the adsorption region 601 of the first adsorption rotor 60 through the exhaust gas inlet pipeline 61 for re-adsorption. In a second embodiment, the other end of the second desorption concentrated gas pipeline 75 is connected to the first cooling gas inlet pipeline 63 (as shown in fig. 2 and 4), so that the concentrated gas can enter the cooling zone 602 of the first adsorption rotor 60 through the first cooling gas inlet pipeline 63 for cooling. Furthermore, the second desorption concentrated gas pipeline 75 is provided with a fan 751 (as shown in fig. 3 and 4) to push and pull the desorption concentrated gas into the waste gas inlet pipeline 61 or the first cooling gas inlet pipeline 63. The desorption gas generated through the desorption region 703 of the second adsorption rotor 70 can enter the adsorption region 601 of the first adsorption rotor 60 or the cooling region 602 of the first adsorption rotor 60 for recycling, so that the organic waste gas treatment efficiency can be improved.

Furthermore, the energy-saving dual-runner high-concentration hot-side bypass over-temperature control system mainly has four embodiments, and the direct-fired incinerator (TO)10, the first heat exchanger 20, the second heat exchanger 30, the third heat exchanger 40, the fourth heat exchanger 50, the first cold-side conveying pipeline 23, the fourth cold-side conveying pipeline 53, the first adsorption runner 60, the second adsorption runner 70 and the chimney 80 in the four 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 third heat exchanger 40, the fourth heat exchanger 50, the first cold-side conveying pipeline 23, the fourth cold-side conveying pipeline 53, the first adsorption runner 60, the second adsorption runner 70 and the chimney 80 are not repeated, and the above description is referred TO.

The difference of the first embodiment (as shown in fig. 1) is that a hot side forced exhaust pipeline 90 is provided at the furnace 102 of the direct-fired incinerator (TO)10, one end of the hot side forced exhaust pipeline 90 is connected TO the furnace 102 of the direct-fired incinerator (TO)10, and the other end of the hot side forced exhaust pipeline 90 is connected TO the connection between the fourth hot side pipeline 52 of the fourth heat exchanger 50 and the third hot side pipeline 42 of the third heat exchanger 40, wherein the hot side forced exhaust pipeline 90 is provided with at least one damper 901, and two dampers (not shown) can be provided in cooperation with the pipeline TO regulate the air volume of the hot side forced exhaust pipeline 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 forced exhaust pipeline 90, and the partially-burned high-temperature gas can be delivered TO the fourth hot side pipeline 52 of the fourth heat exchanger 50 and the third hot side pipeline 42 The connection between the third hot side pipelines 42 of the exchanger 40 allows the hot side forced-discharge pipeline 90 TO have the efficiency of adjusting the heat recovery amount or concentration, so that the direct-fired incinerator (TO)10 can be prevented from generating an over-temperature phenomenon due TO too high incinerator temperature and even from being shut down when organic waste gas is treated.

In addition, the difference of the second embodiment (as shown in fig. 2) is that a hot side forced exhaust pipeline 90 is provided at the furnace chamber 102 of the direct-fired incinerator (TO)10, one end of the hot side forced exhaust pipeline 90 is connected with the furnace chamber 102 of the direct-fired incinerator (TO)10, and the other end of the hot side forced exhaust pipeline 90 is connected with the connection between the third hot side pipeline 42 of the third heat exchanger 40 and the second hot side pipeline 32 of the second heat exchanger 30, wherein the hot side forced exhaust pipeline 90 is provided with at least one damper 901, or two dampers (not shown) can be provided in cooperation with the pipeline, so as TO regulate the air volume of the hot side forced exhaust pipeline 90 through the damper 901, therefore, when the concentration of Volatile Organic Compounds (VOCs) becomes high, the air volume of the furnace chamber 102 of the direct-fired incinerator (TO)10 can be regulated through the forced exhaust pipeline 90, and the partially-burned high-temperature gas can be delivered TO the third hot side pipeline 42 of the third heat exchanger 40 and the second hot side pipeline 32 The connection between the second hot side pipelines 32 of the exchanger 30 allows the hot side forced-exhaust pipeline 90 TO have the efficiency of adjusting the heat recovery amount or concentration, so that the direct-fired incinerator (TO)10 can be prevented from generating an over-temperature phenomenon due TO too high incinerator temperature and even from being shut down when organic waste gas is treated.

In addition, the difference of the third embodiment (as shown in fig. 3) is that a hot side forced exhaust pipeline 90 is provided at the furnace 102 of the direct-fired incinerator (TO)10, one end of the hot side forced exhaust pipeline 90 is connected with the furnace 102 of the direct-fired incinerator (TO)10, and the other end of the hot side forced exhaust pipeline 90 is connected with the connection between the second hot side pipeline 32 of the second heat exchanger 30 and the first hot side pipeline 22 of the first heat exchanger 20, wherein the hot side forced exhaust pipeline 90 is provided with at least one damper 901, or two dampers (not shown) can be provided in cooperation with the pipeline, so as TO regulate the air quantity of the hot side forced exhaust pipeline 90 through the damper 901, therefore, 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 forced exhaust pipeline 90, and the partially-burned high-temperature gas can be delivered TO the second hot side pipeline 32 of the second heat exchanger 30 and the first hot side pipeline 22 of the first heat exchanger 20 The connection between the first hot side pipelines 22 of the exchanger 20 allows the hot side forced exhaust pipeline 90 TO have the efficiency of adjusting the heat recovery amount or concentration, so that the direct-fired incinerator (TO)10 can be prevented from generating an over-temperature phenomenon due TO too high incinerator temperature and even from causing shutdown when organic waste gas is treated.

In addition, the difference of the fourth embodiment (as shown in fig. 4) is that a hot side forced exhaust pipeline 90 is provided in the furnace chamber 102 of the direct-fired incinerator (TO)10, one end of the hot side forced exhaust pipeline 90 is connected TO the furnace chamber 102 of the direct-fired incinerator (TO)10, and the other end of the hot side forced exhaust pipeline 90 is connected TO the outlet 12 of the direct-fired incinerator (TO)10, wherein the hot side forced exhaust pipeline 90 is provided with at least one damper 901, and two dampers (not shown) can be provided in cooperation with the pipeline TO regulate the air volume of the hot side forced exhaust pipeline 90 through the damper 901, so that when the concentration of the Volatile Organic Compounds (VOCs) becomes high, the air volume of the furnace chamber 102 of the direct-fired incinerator (TO)10 can be regulated through the hot side forced exhaust pipeline 90, and the partially burnt high-temperature gas can be delivered TO the outlet 12 of the direct-fired incinerator (TO)10, the hot side forced exhaust pipeline 90 has the efficiency of adjusting the heat recovery amount or concentration, so that the direct combustion type incinerator (TO)10 can be prevented from being overheated due TO too high incinerator temperature and even being shut down when organic waste gas is treated.

The energy-saving double-runner high-concentration hot-side bypass over-temperature control method of the invention is mainly used for an organic waste gas treatment system, and comprises a combined design of a direct-fired incinerator (TO)10, a first heat exchanger 20, a second heat exchanger 30, a third heat exchanger 40, a fourth heat exchanger 50, a first cold-side conveying pipeline 23, a fourth cold-side conveying pipeline 53, a first adsorption runner 60, a second adsorption runner 70 and a chimney 80 (as shown in figures 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, the third heat exchanger 40 is provided with a third cold-side pipeline 41 and a third hot-side pipeline 42, the fourth heat exchanger 50 is provided with a fourth cold-side pipeline 51 and a fourth hot-side pipeline 52, wherein 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 transfer pipe 23 is connected TO one end of the fourth cold-side pipe 51, one end of the fourth cold-side transfer pipe 53 is connected TO the other end of the fourth cold-side pipe 51, and the other end of the fourth cold-side transfer pipe 53 is connected TO the inlet 11 of the direct-fired incinerator (TO) 10. The direct-fired incinerator (TO)10 is provided with a burner 101 and a furnace chamber 102, the furnace end 101 is communicated with the furnace chamber 102, and the first heat exchanger 20, the second heat exchanger 30, the third heat exchanger 40 and the fourth heat exchanger 50 are respectively arranged in the direct-fired incinerator (TO)10, and the direct combustion incinerator (TO)10 is provided with an inlet 11 and an outlet 12 (as shown in fig. 1 TO 4), and the inlet 11 is provided at the burner 101, and the inlet 11 is connected to the other end of the fourth cold-side pipe 51 of the fourth heat exchanger 50, and, furthermore, the outlet 12 is disposed at the furnace 102, and the outlet 12 is connected to 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 102 and be discharged from the outlet 12 to the chimney 80 for discharge, thereby saving energy.

The first adsorption rotor 60 of the present invention is provided with an adsorption zone 601, a cooling zone 602 and a desorption zone 603, the first adsorption rotor 60 is connected to a waste gas inlet line 61, a first clean gas discharge line 62, a first cooling gas inlet line 63, a first cooling gas delivery line 64, a first hot gas delivery line 65 and a first desorption concentrated gas line 66 (as shown in fig. 1 to 4), the second adsorption rotor 70 is provided with an adsorption zone 701, a cooling zone 702 and a desorption zone 703, and the second adsorption rotor 70 is connected to a second clean gas discharge line 71, a second cooling gas inlet line 72, a second cooling gas delivery line 73, a second hot gas delivery line 74 and a second desorption concentrated gas line 75 (as shown in fig. 1 to 4). Wherein the first adsorption rotor 60 and the second adsorption rotor 70 are zeolite concentration rotors or other material concentration rotors, respectively.

The main steps of the control method (as shown in fig. 5) include: step S100 inputs gas to be adsorbed: the exhaust gas is fed into one side of the adsorption zone 601 of the first 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.

In addition, the next step is that the first adsorption wheel adsorbs in step S110: after being adsorbed by the adsorption region 601 of the first adsorption rotor 60, the adsorbed gas is output from the other side of the adsorption region 601 of the first adsorption rotor 60 to the adsorption region 701 of the second adsorption rotor 70 through the other end of the first purified gas discharge line 62. After the step S110 is completed, the next step S120 is performed.

The other side of the adsorption region 701 of the second adsorption rotating wheel 70 in the step S110 is connected to the second purified gas discharge pipeline 71, so as to be connected to the chimney 80 through the other end of the second purified gas discharge pipeline 71, and the second purified gas discharge pipeline 71 is provided with a fan 711 (as shown in fig. 3 and 4), so that the fan 711 can push and pull the adsorbed gas in the second purified gas discharge pipeline 71 into the chimney 80 for discharge.

Further, the next step proceeds to step S120 of inputting the first cooling gas: the cooling air is supplied to the cooling zone 602 of the first adsorption rotor 60 through the other end of the first cooling air inlet pipe 63 for cooling, and the cooling air passing through the cooling zone 602 of the first adsorption rotor 60 is supplied to one end of the third cold-side pipe 41 of the third heat exchanger 40 through the other end of the first cooling air supply pipe 64. After the step S120 is completed, the next step S130 is performed.

In the step S120, the cooling area 602 of the first sorption rotor 60 has two embodiments, wherein in the first embodiment, the first cooling air inlet pipeline 63 connected to one side of the cooling area 602 of the first sorption rotor 60 is used for entering fresh air or external air (as shown in fig. 1), and the cooling area 602 of the first sorption rotor 60 is provided by the fresh air or the external air for cooling. In another 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 first cooling gas inlet pipe 63 (as shown in fig. 3) so as to convey the exhaust gas in the exhaust gas inlet pipe 61 to the cooling zone 602 of the first 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 for controlling the air volume of the exhaust gas communication pipe 611.

In addition, the next step is step S130 of delivering a first hot gas for desorption: the hot gas is delivered to the desorption region 603 of the first adsorption rotor 60 for desorption through the first hot gas delivery line 65 connected to the other end of the third cold-side line 41 of the third heat exchanger 40, and the 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 first desorption concentrated gas line 66. After the step S130 is completed, the next step S140 is performed.

The first 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.

Further, the next step, step S140, is to desorb the concentrated gas delivery: the desorbed concentrated gas is further transferred TO one end of the fourth cold-side pipe 51 of the fourth heat exchanger 50 through the first cold-side transfer pipe 23 TO which the other end of the first cold-side pipe 21 of the first heat exchanger 20 is connected, and is further transferred TO the inlet 11 of the direct combustion incinerator (TO)10 through the fourth cold-side transfer pipe 53 TO which the other end of the fourth cold-side pipe 51 of the fourth heat exchanger 50 is connected. After the step S140 is completed, the next step S150 is performed.

Further, the next step is gas transport after incineration in step S150: the burned gas generated after being burned by the burner 101 of the direct combustion type incinerator (TO)10 is transferred TO one end of the fourth hot side pipe 52 of the fourth heat exchanger 50, and is transferred TO one end of the third hot side pipe 42 of the third heat exchanger 40 by the other end of the fourth hot side pipe 52 of the fourth heat exchanger 50, and is transferred TO one end of the second hot side pipe 32 of the second heat exchanger 30 by the other end of the third hot side pipe 42 of the third heat exchanger 40, is 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 is 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.

In addition, the next step is that the second adsorption wheel adsorbs: the gas adsorbed in the first purified gas discharge pipeline 62 is transported to one side of the adsorption region 701 of the second adsorption rotor 70 for adsorption, and the gas adsorbed for the second time is transported to the chimney 80 through the second purified gas discharge pipeline 71 for discharge. After the step S160 is completed, the next step S170 is performed.

Further, the next step proceeds to step S170 of inputting a second cooling gas: the cooling air is supplied to the cooling zone 702 of the second sorption rotor 70 for cooling through the other end of the second cooling air inlet conduit 72, and the cooling air passing through the cooling zone 702 of the second sorption rotor 70 is supplied to one end of the second cold side conduit 31 of the second heat exchanger 30 through the other end of the second cooling air supply conduit 73. After the step S170 is completed, the next step S180 is performed.

In the above step S170, the cooling zone 702 of the second sorption rotor 70 has two embodiments, wherein in the first embodiment, the second cooling air inlet pipe 72 connected to one side of the cooling zone 702 of the second sorption rotor 70 is used for introducing fresh air or external air (as shown in fig. 1), and the cooling zone 702 of the second sorption rotor 70 is cooled by the fresh air or the external air. In another second embodiment, the first net gas discharging pipeline 62 is provided with a first net gas communicating pipeline 621, and the other end of the first net gas communicating pipeline 621 is connected to the second cooling gas inlet pipeline 72 (as shown in fig. 3 and fig. 4) so as to convey the gas in the first net gas discharging pipeline 62 to the cooling zone 702 of the second adsorption rotating wheel 70 for cooling through the first net gas communicating pipeline 621, and the first net gas communicating pipeline 621 is provided with a first net gas communicating control valve 6211 so as to control the air volume of the first net gas communicating pipeline 621.

In addition, the next step is that step S180 is to deliver a second hot gas desorption: the hot gas is delivered to the desorption region 703 of the second adsorption rotor 70 for desorption through a second hot gas delivery line 74 connected to the other end of the second cold-side line 31 of the second heat exchanger 30, and is then outputted through the other end of the second desorption concentrated gas line 75. After the step S180 is completed, the next step S190 is performed.

There are two embodiments of the other end of the second desorption concentrated gas pipeline 75 in the step S180, and the first embodiment is that the other end of the second desorption concentrated gas pipeline 75 is connected to the waste gas inlet pipeline 61 (as shown in fig. 1 and fig. 3), so that the concentrated gas can enter the adsorption area 601 of the first adsorption rotor 60 through the waste gas inlet pipeline 61 again for re-adsorption. In a second embodiment, the other end of the second desorption concentrated gas pipeline 75 is connected to the first cooling gas inlet pipeline 63 (as shown in fig. 2 and 4), so that the concentrated gas can enter the cooling zone 602 of the first adsorption rotor 60 through the first cooling gas inlet pipeline 63 for cooling. Furthermore, the second desorption concentrated gas pipeline 75 is provided with a fan 751 for pushing and pulling the desorption concentrated gas into the waste gas inlet pipeline 61 or the first cooling gas inlet pipeline 63. The desorption gas generated through the desorption region 703 of the second adsorption rotor 70 can enter the adsorption region 601 of the first adsorption rotor 60 or the cooling region 602 of the first adsorption rotor 60 for recycling, so that the organic waste gas treatment efficiency can be improved.

In addition, next step S190 hot side forced exhaust pipeline adjustment: the hearth 102 of the direct-fired incinerator (TO)10 is provided with a hot-side forced exhaust pipeline 90, one end of the hot-side forced exhaust pipeline 90 is connected with the hearth 102 of the direct-fired incinerator (TO)10, the other end of the hot-side forced exhaust pipeline 90 is connected with a connection part between the fourth hot-side pipeline 52 of the fourth heat exchanger 50 and the third hot-side pipeline 42 of the third heat exchanger 40, and the hot-side forced exhaust pipeline 90 is provided with at least one damper 901 TO regulate the air volume of the hearth 102 of the direct-fired incinerator (TO)10 through the hot-side forced exhaust pipeline 90.

Wherein in the step S190, one end of the hot-side forced exhaust pipeline 90 is connected TO the furnace chamber 102 of the direct-fired incinerator (TO)10, and the other end of the hot-side forced exhaust pipeline 90 is connected TO the connection between the fourth hot-side pipeline 52 of the fourth heat exchanger 50 and the third hot-side pipeline 42 of the third heat exchanger 40, wherein the hot-side forced exhaust pipeline 90 is provided with at least one damper 901, and two dampers (not shown) can be provided in cooperation with the pipeline TO regulate the air volume of the hot-side forced exhaust pipeline 90 through the damper 901, so that when the concentration of Volatile Organic Compounds (VOCs) becomes high, the air volume of the furnace chamber 102 of the direct-fired incinerator (TO)10 can be regulated through the hot-side forced exhaust pipeline 90, and part of the burned high-temperature gas can be delivered TO the connection between the fourth hot-side pipeline 52 of the fourth heat exchanger 50 and the third hot-side pipeline 42 of the third heat exchanger 40, the hot side forced exhaust pipeline 90 has the efficiency of adjusting the heat recovery amount or concentration, so that the direct combustion type incinerator (TO)10 can be prevented from being overheated due TO too high incinerator temperature and even being shut down when organic waste gas is treated.

Furthermore, the energy-saving dual-rotor high-concentration hot-side bypass over-temperature control method of the present invention mainly includes four embodiments, and the first embodiment (as shown in fig. 5) includes step S100 of inputting a gas to be adsorbed, step S110 of adsorbing by the first adsorption rotor, step S120 of inputting a first cooling gas, step S130 of delivering a first hot gas for desorption, step S140 of delivering a concentrated desorption gas, step S150 of delivering a burned gas, step S160 of adsorbing by the second adsorption rotor, step S170 of inputting a second cooling gas, step S180 of delivering a second hot gas for desorption, and step S190 of regulating a hot-side forced exhaust pipeline, which has 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 first adsorption wheel is used for adsorption in step S210, the first cooling gas is input in step S220, the first hot gas is transmitted for desorption in step S230, the concentrated gas is desorbed in step S240, the gas after incineration in step S250 is transmitted, the second adsorption wheel is used for adsorption in step S260, the second cooling gas is input in step S270 and the second hot gas is transmitted in step S280 for desorption, and the gas to be adsorbed is input in step S300, the first adsorption wheel is used for adsorption in step S310, the first cooling gas is input in step S320, the first hot gas is transmitted in step S330, the concentrated gas is desorbed in step S340, the gas after incineration in step S350, the second adsorption wheel is used for adsorption in step S360, the second cooling gas is input in step S370 and the second cooling gas is transmitted in step S380, and the gas to be adsorbed is input in step S400, the gas after incineration in step S340, the desorption in the fourth embodiment (as shown in fig. 8), The steps S410 of adsorbing by the first adsorption rotor, S420 of inputting the first cooling gas, S430 of delivering the first hot gas for desorption, S440 of desorbing and delivering the concentrated gas, S450 of incinerating the gas, S460 of adsorbing by the second adsorption rotor, S470 of inputting the second cooling gas, and S480 of delivering the second hot gas for desorption are the same designs as the steps S100 of inputting the gas to be adsorbed, S110 of adsorbing by the first adsorption rotor, S120 of inputting the first cooling gas, S130 of delivering the first hot gas for desorption, S140 of desorbing and delivering the concentrated gas, S150 of incinerating the gas, S160 of adsorbing by the second adsorption rotor, S170 of inputting the second cooling gas, and S180 of delivering the second hot gas for desorption in the first embodiment (as shown in fig. 5), and the difference lies in the content of the adjustment of the hot side forced exhaust pipeline of S190.

Therefore, the same contents as the steps of inputting the gas to be adsorbed in step S100, adsorbing by the first adsorption rotor in step S110, inputting the first cooling gas in step S120, delivering the first hot gas for desorption in step S130, delivering the concentrated gas for desorption in step S140, delivering the burned gas in step S150, adsorbing by the second adsorption rotor in step S160, inputting the second cooling gas in step S170, and delivering the second hot gas for desorption in step S180 are not repeated, and please refer to the above description. The following description will be made with respect to the hot side forced exhaust pipe adjustment at step S290 in the second embodiment (shown in fig. 6), the hot side forced exhaust pipe adjustment at step S390 in the third embodiment (shown in fig. 7), and the hot side forced exhaust pipe adjustment at step S490 in the fourth embodiment (shown in fig. 8).

The difference of the second embodiment (as shown in fig. 6) is that in step S290, the hot side forced exhaust pipeline is adjusted: the hearth 102 of the direct-fired incinerator (TO)10 is provided with a hot-side forced exhaust pipeline 90, one end of the hot-side forced exhaust pipeline 90 is connected with the hearth 102 of the direct-fired incinerator (TO)10, the other end of the hot-side forced exhaust pipeline 90 is connected with a connection part between the third hot-side pipeline 42 of the third heat exchanger 40 and the second hot-side pipeline 32 of the second heat exchanger 30, and the hot-side forced exhaust pipeline 90 is provided with at least one damper 901 TO regulate the air volume of the hearth 102 of the direct-fired incinerator (TO)10 through the hot-side forced exhaust pipeline 90.

Wherein in the step S290, one end of the hot-side forced exhaust pipeline 90 is connected TO the furnace chamber 102 of the direct-fired incinerator (TO)10, and the other end of the hot-side forced exhaust pipeline 90 is connected TO the connection between the third hot-side pipeline 42 of the third heat exchanger 40 and the second hot-side pipeline 32 of the second heat exchanger 30, wherein the hot-side forced exhaust pipeline 90 is provided with at least one damper 901, and two dampers (not shown) can be provided in cooperation with the pipeline TO regulate the air volume of the hot-side forced exhaust pipeline 90 through the damper 901, so that when the concentration of Volatile Organic Compounds (VOCs) becomes high, the air volume of the furnace chamber 102 of the direct-fired incinerator (TO)10 can be regulated through the hot-side forced exhaust pipeline 90, and part of the burned high-temperature gas can be delivered TO the connection between the third hot-side pipeline 42 of the third heat exchanger 40 and the second hot-side pipeline 32 of the second heat exchanger 30, the hot side forced exhaust pipeline 90 has the efficiency of adjusting the heat recovery amount or concentration, so that the direct combustion type incinerator (TO)10 can be prevented from being overheated due TO too high incinerator temperature and even being shut down when organic waste gas is treated.

The difference between the third embodiment (as shown in fig. 7) is that in step S390, the hot side forced exhaust pipeline is adjusted: the hearth 102 of the direct-fired incinerator (TO)10 is provided with a hot-side forced exhaust pipeline 90, one end of the hot-side forced exhaust pipeline 90 is connected with the hearth 102 of the direct-fired incinerator (TO)10, the other end of the hot-side forced exhaust pipeline 90 is connected with a connection part between the second hot-side pipeline 32 of the second heat exchanger 30 and the first hot-side pipeline 22 of the first heat exchanger 20, and the hot-side forced exhaust pipeline 90 is provided with at least one damper 901 TO regulate the air volume of the hearth 102 of the direct-fired incinerator (TO)10 through the hot-side forced exhaust pipeline 90.

Wherein in the step S390, one end of the hot-side forced exhaust pipeline 90 is connected TO the furnace chamber 102 of the direct-fired incinerator (TO)10, and the other end of the hot-side forced exhaust pipeline 90 is connected TO the connection between the second hot-side pipeline 32 of the second heat exchanger 30 and the first hot-side pipeline 22 of the first heat exchanger 20, wherein the hot-side forced exhaust pipeline 90 is provided with at least one damper 901, and two dampers (not shown) can be provided in cooperation with the pipeline TO regulate the air volume of the hot-side forced exhaust pipeline 90 through the damper 901, so that when the concentration of Volatile Organic Compounds (VOCs) becomes high, the air volume of the furnace chamber 102 of the direct-fired incinerator (TO)10 can be regulated through the hot-side forced exhaust pipeline 90, and part of the burned high-temperature gas can be delivered TO the connection between the second hot-side pipeline 32 of the second heat exchanger 30 and the first hot-side pipeline 22 of the first heat exchanger 20, the hot side forced exhaust pipeline 90 has the efficiency of adjusting the heat recovery amount or concentration, so that the direct combustion type incinerator (TO)10 can be prevented from being overheated due TO too high incinerator temperature and even being shut down when organic waste gas is treated.

Furthermore, the difference of the fourth embodiment (as shown in fig. 8) is that in step S490, the hot side forced exhaust pipeline is adjusted: the hearth 102 of the direct-fired incinerator (TO)10 is provided with a hot-side forced exhaust pipeline 90, one end of the hot-side forced exhaust pipeline 90 is connected with the hearth 102 of the direct-fired incinerator (TO)10, the other end of the hot-side forced exhaust pipeline 90 is connected with the outlet 12 of the direct-fired incinerator (TO)10, and the hot-side forced exhaust pipeline 90 is provided with at least one air damper 901 TO adjust the air volume of the hearth 102 of the direct-fired incinerator (TO)10 through the hot-side forced exhaust pipeline 90.

Wherein in the step S490, one end of the hot side forced exhaust pipeline 90 is connected TO the furnace chamber 102 of the direct-fired incinerator (TO)10, and the other end of the hot side forced exhaust pipeline 90 is connected TO the outlet 12 of the direct-fired incinerator (TO)10, wherein the hot side forced exhaust pipeline 90 is provided with at least one damper 901, or two dampers (not shown) can be provided in combination with the pipeline, so as TO regulate the air volume of the hot side forced exhaust pipeline 90 through the damper 901, therefore, when the concentration of Volatile Organic Compounds (VOCs) becomes high, the air volume of the furnace chamber 102 of the direct-fired incinerator (TO)10 can be regulated through the hot side forced exhaust pipeline 90, and part of the burned high-temperature gas is delivered TO the outlet 12 of the hot side forced exhaust pipeline (TO)10, so that the forced exhaust pipeline 90 has the efficiency of regulating the heat recovery amount or concentration, so that the organic waste gas can be treated, the direct-fired incinerator (TO)10 can be prevented from being overheated due TO too high incinerator temperature and even being shut down.

From the above detailed description, it will be apparent to those skilled in the art that the foregoing objects and advantages of the present invention are achieved, and the invention has been filed in accordance with the provisions of the patent statutes.

However, the above description is only a preferred embodiment of the present invention, and the scope of the present invention should not be limited thereby; therefore, all the equivalent changes and modifications made by the claims and the content of the specification of the invention should be covered by the scope of the patent of the invention.

Claims

1. An energy-saving double-runner high-concentration hot-side bypass over-temperature control system comprises:

the direct-fired incinerator is provided with a furnace end and a hearth, the furnace end is communicated with the hearth, the direct-fired incinerator is provided with an inlet and an outlet, the inlet is arranged at the furnace end, and the outlet is arranged at the hearth;

the first heat exchanger is arranged in the direct-fired incinerator and is provided with a first cold-side pipeline and a first hot-side pipeline;

the second heat exchanger is arranged in the direct-fired incinerator and is provided with a second cold side pipeline and a second hot side pipeline;

the third heat exchanger is arranged in the direct-fired incinerator and is provided with a third cold-side pipeline and a third hot-side pipeline;

the fourth heat exchanger is arranged in the direct-fired incinerator and is provided with a fourth cold-side pipeline and a fourth hot-side pipeline;

the first cold side conveying pipeline is connected with one end of the fourth cold side pipeline at one end;

one end of the fourth cold-side conveying pipeline is connected with the other end of the fourth cold-side pipeline, and the other end of the fourth cold-side conveying pipeline is connected with an inlet of the direct-fired incinerator;

a first adsorption rotating wheel, the first adsorption rotating wheel is provided with an adsorption area, a cooling area and a desorption area, the first adsorption rotating wheel is connected with a waste gas inlet pipeline, a first purified gas discharge pipeline, a first cooling gas inlet pipeline, a first cooling gas conveying pipeline, a first hot gas conveying pipeline and a first desorption concentrated gas pipeline, one end of the waste gas inlet pipeline is connected to one side of the adsorption area of the first adsorption rotating wheel, one end of the first purified gas discharge pipeline is connected with the other side of the adsorption area of the first adsorption rotating wheel, one end of the first cooling gas inlet pipeline is connected with one side of the cooling area of the first adsorption rotating wheel, one end of the first cooling gas conveying pipeline is connected with the other side of the cooling area of the first adsorption rotating wheel, the other end of the first cooling gas conveying pipeline is connected with one end of a third cold side pipeline of the third heat exchanger, one end of the first hot gas conveying pipeline is connected with the other side of the desorption area of the first adsorption rotating wheel, the other end of the first hot gas conveying pipeline is connected with the other end of a third cold side pipeline of the third heat exchanger, one end of the first desorption concentrated gas pipeline is connected with one side of the desorption area of the first adsorption rotating wheel, and the other end of the first desorption concentrated gas pipeline is connected with one end of the first cold side pipeline of the first heat exchanger;

a second adsorption rotating wheel, which is provided with an adsorption zone, a cooling zone and a desorption zone, the second adsorption rotating wheel is connected with a second purified gas discharge pipeline, a second cooling gas inlet pipeline, a second cooling gas conveying pipeline, a second hot gas conveying pipeline and a second desorption concentrated gas pipeline, one end of the first purified gas discharge pipeline is connected to one side of the adsorption zone of the second adsorption rotating wheel, one end of the second purified gas discharge pipeline is connected with the other side of the adsorption zone of the second adsorption rotating wheel, one end of the second cooling gas inlet pipeline is connected with one side of the cooling zone of the second adsorption rotating wheel, one end of the second cooling gas conveying pipeline is connected with the other side of the cooling zone of the second adsorption rotating wheel, the other end of the second cooling gas conveying pipeline is connected with one end of the second cold side pipeline of the second heat exchanger, one end of the second hot gas conveying pipeline is connected with the other side of the desorption zone of the second adsorption rotating wheel, the other end of the second hot gas conveying pipeline is connected with the other end of a second cold side pipeline of the second heat exchanger, and one end of the second desorption concentrated gas pipeline is connected with one side of a desorption area of the second adsorption rotating wheel;

the other end of the second purified gas discharge pipeline is connected with the chimney; and

and one end of the hot side forced exhaust pipeline is connected with the hearth of the direct-fired incinerator, the other end of the hot side forced exhaust pipeline is connected with a connection part between a fourth hot side pipeline of the fourth heat exchanger and a third hot side pipeline of the third heat exchanger, and the hot side forced exhaust pipeline is provided with at least one air damper.

2. An energy-saving double-runner high-concentration hot-side bypass over-temperature control system comprises:

and one end of the hot side forced exhaust pipeline is connected with the hearth of the direct-fired incinerator, the other end of the hot side forced exhaust pipeline is connected with a joint between a third hot side pipeline of the third heat exchanger and a second hot side pipeline of the second heat exchanger, and the hot side forced exhaust pipeline is provided with at least one air damper.

3. An energy-saving double-runner high-concentration hot-side bypass over-temperature control system comprises:

and one end of the hot side forced exhaust pipeline is connected with the hearth of the direct-fired incinerator, the other end of the hot side forced exhaust pipeline is connected with the joint between the second hot side pipeline of the second heat exchanger and the first hot side pipeline of the first heat exchanger, and the hot side forced exhaust pipeline is provided with at least one air damper.

4. An energy-saving double-runner high-concentration hot-side bypass over-temperature control system comprises:

a second adsorption rotating wheel, which is provided with an adsorption zone, a cooling zone and a desorption zone, the second adsorption rotating wheel is connected with a second clean gas discharge pipeline, a second cooling gas inlet pipeline, a second cooling gas conveying pipeline, a second hot gas conveying pipeline and a second desorption concentrated gas pipeline, one end of the first clean gas discharge pipeline is connected to one side of the adsorption zone of the second adsorption rotating wheel, one end of the second clean gas discharge pipeline is connected with the other side of the adsorption zone of the second adsorption rotating wheel, one end of the second cooling gas inlet pipeline is connected with one side of the second adsorption rotating wheel, one end of the second cooling gas conveying pipeline is connected with the other side of the cooling zone of the second adsorption rotating wheel, the other end of the second cooling gas conveying pipeline is connected with one end of the second cold side pipeline of the second heat exchanger, one end of the second hot gas conveying pipeline is connected with the other side of the second adsorption rotating wheel, the other end of the second hot gas conveying pipeline is connected with the other end of a second cold side pipeline of the second heat exchanger, and one end of the second desorption concentrated gas pipeline is connected with one side of a desorption area of the second adsorption rotating wheel;

one end of the hot side forced exhaust pipeline is connected with the hearth of the direct-fired incinerator, the other end of the hot side forced exhaust pipeline is connected with the outlet of the direct-fired incinerator, and the hot side forced exhaust pipeline is provided with at least one air adjusting door.

5. The energy efficient dual-spool high-consistency hot-side bypass over-temperature control system of claim 1, 2, 3, or 4, wherein the outlet of the direct-fired incinerator is connected to the chimney.

6. The energy efficient dual-spool high-concentration hot-side bypass over-temperature control system as claimed in claim 1, 2, 3 or 4, wherein the first cooling air intake duct is for fresh air or outside air.

7. The energy efficient dual-spool high-concentration hot-side bypass over-temperature control system as claimed in claim 1, 2, 3 or 4, wherein the second cooling air intake duct is for fresh air or outside air.

8. The energy-saving type double-runner high-concentration hot-side bypass over-temperature control system as claimed in claim 1, 2, 3 or 4, wherein the exhaust gas inlet pipeline is provided with an exhaust gas communication pipeline, the exhaust gas communication pipeline is connected with the first cooling gas inlet pipeline, and the exhaust gas communication pipeline is provided with an exhaust gas communication control valve to control the air volume of the exhaust gas communication pipeline.

9. The energy-saving dual-runner high-concentration hot-side bypass over-temperature control system as claimed in claim 1, 2, 3 or 4, wherein the first net gas discharge pipeline is provided with a first net gas communication pipeline, the first net gas communication pipeline is connected to the second cooling gas inlet pipeline, and the first net gas communication pipeline is provided with a first net gas communication control valve for controlling the air volume of the first net gas communication pipeline.

10. The energy-saving dual-runner high-concentration hot-side bypass over-temperature control system as claimed in claim 1, 2, 3 or 4, wherein the first desorption concentrated gas pipeline is provided with a fan.

11. The energy-saving dual-runner high-concentration hot-side bypass over-temperature control system as claimed in claim 1, 2, 3 or 4, wherein the second desorption concentrated gas pipeline is provided with a fan.

12. The energy efficient dual-spool high-concentration hot-side bypass over-temperature control system as claimed in claim 1, 2, 3 or 4, wherein the second net gas discharge pipeline is provided with a fan.

13. The energy-saving double-runner high-concentration hot-side bypass over-temperature control system as claimed in claim 1, 2, 3 or 4, wherein the other end of the second desorption concentrated gas pipeline is connected with the exhaust gas inlet pipeline.

14. The energy-saving double-runner high-concentration hot-side bypass over-temperature control system as claimed in claim 1, 2, 3 or 4, wherein the other end of the second desorption concentrated gas pipeline is connected with the first cooling gas inlet pipeline.

15. An energy-saving double-runner high-concentration hot-side bypass over-temperature control method is mainly used for an organic waste gas treatment system and is provided with a direct-fired incinerator, a first heat exchanger, a second heat exchanger, a third heat exchanger, a fourth heat exchanger, a first cold-side conveying pipeline, a fourth cold-side conveying pipeline, a first adsorption rotating wheel, a second adsorption rotating wheel and a chimney, wherein the direct-fired incinerator is provided with a burner and a hearth, the burner is communicated with the hearth, the direct-fired incinerator is provided with an inlet and an outlet, the inlet is arranged at the burner, the outlet is arranged at the hearth, 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, the third heat exchanger is provided with a third cold-side pipeline and a third hot-side pipeline, the fourth heat exchanger is provided with a fourth cold-side pipeline and a fourth hot-side pipeline, one end of a 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 one end of a fourth cold-side pipeline, one end of the fourth cold-side conveying pipeline is connected with the other end of the fourth cold-side pipeline, the other end of the fourth cold-side conveying pipeline is connected with an inlet of the direct-fired incinerator, the first adsorption rotating wheel is provided with an adsorption zone, a cooling zone and a desorption zone, the first adsorption rotating wheel is connected with a waste gas inlet pipeline, a first clean gas discharge pipeline, a first cooling gas inlet pipeline, a first cooling gas conveying pipeline, a first hot gas conveying pipeline and a first desorption concentrated gas pipeline, the second adsorption rotating wheel is provided with an adsorption zone, a cooling zone and a desorption zone, and the second adsorption rotating wheel is connected with a second clean gas discharge pipeline, a second cooling gas inlet pipeline and a second cooling gas conveying pipeline, A second hot gas delivery pipeline and a second desorption concentrated gas pipeline, and the control method mainly comprises the following steps:

input of gas to be adsorbed: sending waste gas to one side of the adsorption area of the first adsorption runner through the other end of the waste gas inlet pipeline;

the first adsorption runner adsorbs: after the gas is adsorbed by the adsorption area of the first adsorption runner, the gas after adsorption is output to the adsorption area of the second adsorption runner from the other side of the adsorption area of the first adsorption runner through the other end of the first purified gas discharge pipeline;

inputting a first cooling gas: conveying cooling air to the cooling area of the first adsorption rotor for cooling through the other end of the first cooling air inlet pipeline, and conveying the cooling air passing through the cooling area of the first adsorption rotor to one end of a third cold-side pipeline of the third heat exchanger through the other end of the first cooling air conveying pipeline;

conveying a first hot gas for desorption: the hot gas is conveyed to the desorption area of the first adsorption runner for desorption through a first hot gas conveying pipeline connected with the other end of the third cold side pipeline of the third heat exchanger, and then the 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 first desorption concentrated gas pipeline;

and (3) desorption and concentrated gas conveying: the desorbed concentrated gas is conveyed to one end of a fourth cold-side pipeline of the fourth heat exchanger through a first cold-side conveying pipeline connected with the other end of the first cold-side pipeline of the first heat exchanger, and is conveyed to an inlet of the direct-fired incinerator through a fourth cold-side conveying pipeline connected with the other end of the fourth cold-side pipeline of the fourth heat exchanger;

conveying gas after incineration: conveying incinerated gas generated after combustion of a furnace end of the direct-fired incinerator to one end of a fourth hot-side pipeline of the fourth heat exchanger, conveying the incinerated gas to one end of a third hot-side pipeline of the third heat exchanger from the other end of the fourth hot-side pipeline of the fourth 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 third hot-side pipeline of the third heat exchanger, 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 from the other end of the first hot-side pipeline of the first heat exchanger;

and (3) adsorption by a second adsorption rotating wheel: conveying the gas adsorbed in the first purified gas discharge pipeline to one side of an adsorption area of the second adsorption rotating wheel for adsorption, and conveying the gas adsorbed for the second time to a chimney for discharge through the second purified gas discharge pipeline;

inputting a second cooling gas: conveying cooling gas to the cooling area of the second adsorption rotating wheel for cooling through the other end of the second cooling gas inlet pipeline, and conveying the cooling gas passing through the cooling area of the second adsorption rotating wheel to one end of a second cold side pipeline of the second heat exchanger through the other end of the second cooling gas conveying pipeline;

and (3) conveying a second hot gas for desorption: the hot gas is conveyed to the desorption area of the second adsorption rotating wheel for desorption through a second hot gas conveying pipeline connected with the other end of a second cold side pipeline of the second heat exchanger, and then the hot gas is output through the other end of the second desorption concentrated gas pipeline; and

and (3) hot side forced exhaust pipeline adjustment: the hearth of the direct-fired incinerator is provided with a hot-side forced exhaust pipeline, one end of the hot-side forced exhaust pipeline is connected with the hearth of the direct-fired incinerator, the other end of the hot-side forced exhaust pipeline is connected with a joint between a fourth hot-side pipeline of the fourth heat exchanger and a third hot-side pipeline of the third heat exchanger, and the hot-side forced exhaust pipeline is provided with at least one air adjusting door so as to adjust the air volume of the hearth of the direct-fired incinerator through the hot-side forced exhaust pipeline.

16. An energy-saving double-runner high-concentration hot-side bypass over-temperature control method is mainly used for an organic waste gas treatment system and is provided with a direct-fired incinerator, a first heat exchanger, a second heat exchanger, a third heat exchanger, a fourth heat exchanger, a first cold-side conveying pipeline, a fourth cold-side conveying pipeline, a first adsorption rotating wheel, a second adsorption rotating wheel and a chimney, wherein the direct-fired incinerator is provided with a burner and a hearth, the burner is communicated with the hearth, the direct-fired incinerator is provided with an inlet and an outlet, the inlet is arranged at the burner, the outlet is arranged at the hearth, 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, the third heat exchanger is provided with a third cold-side pipeline and a third hot-side pipeline, the fourth heat exchanger is provided with a fourth cold-side pipeline and a fourth hot-side pipeline, one end of a 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 one end of a fourth cold-side pipeline, one end of the fourth cold-side conveying pipeline is connected with the other end of the fourth cold-side pipeline, the other end of the fourth cold-side conveying pipeline is connected with an inlet of the direct-fired incinerator, the first adsorption rotating wheel is provided with an adsorption zone, a cooling zone and a desorption zone, the first adsorption rotating wheel is connected with a waste gas inlet pipeline, a first clean gas discharge pipeline, a first cooling gas inlet pipeline, a first cooling gas conveying pipeline, a first hot gas conveying pipeline and a first desorption concentrated gas pipeline, the second adsorption rotating wheel is provided with an adsorption zone, a cooling zone and a desorption zone, and the second adsorption rotating wheel is connected with a second clean gas discharge pipeline, a second cooling gas inlet pipeline and a second cooling gas conveying pipeline, A second hot gas delivery pipeline and a second desorption concentrated gas pipeline, and the control method mainly comprises the following steps:

and (3) hot side forced exhaust pipeline adjustment: the hearth of the direct-fired incinerator is provided with a hot-side forced exhaust pipeline, one end of the hot-side forced exhaust pipeline is connected with the hearth of the direct-fired incinerator, the other end of the hot-side forced exhaust pipeline is connected with a joint between a third hot-side pipeline of the third heat exchanger and a second hot-side pipeline of the second heat exchanger, and the hot-side forced exhaust pipeline is provided with at least one air adjusting door so as to adjust the air volume of the hearth of the direct-fired incinerator through the hot-side forced exhaust pipeline.

17. An energy-saving double-runner high-concentration hot-side bypass over-temperature control method is mainly used for an organic waste gas treatment system and is provided with a direct-fired incinerator, a first heat exchanger, a second heat exchanger, a third heat exchanger, a fourth heat exchanger, a first cold-side conveying pipeline, a fourth cold-side conveying pipeline, a first adsorption rotating wheel, a second adsorption rotating wheel and a chimney, wherein the direct-fired incinerator is provided with a burner and a hearth, the burner is communicated with the hearth, the direct-fired incinerator is provided with an inlet and an outlet, the inlet is arranged at the burner, the outlet is arranged at the hearth, 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, the third heat exchanger is provided with a third cold-side pipeline and a third hot-side pipeline, the fourth heat exchanger is provided with a fourth cold-side pipeline and a fourth hot-side pipeline, one end of a 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 one end of a fourth cold-side pipeline, one end of the fourth cold-side conveying pipeline is connected with the other end of the fourth cold-side pipeline, the other end of the fourth cold-side conveying pipeline is connected with an inlet of the direct-fired incinerator, the first adsorption rotating wheel is provided with an adsorption zone, a cooling zone and a desorption zone, the first adsorption rotating wheel is connected with a waste gas inlet pipeline, a first clean gas discharge pipeline, a first cooling gas inlet pipeline, a first cooling gas conveying pipeline, a first hot gas conveying pipeline and a first desorption concentrated gas pipeline, the second adsorption rotating wheel is provided with an adsorption zone, a cooling zone and a desorption zone, and the second adsorption rotating wheel is connected with a second clean gas discharge pipeline, a second cooling gas inlet pipeline and a second cooling gas conveying pipeline, A second hot gas delivery pipeline and a second desorption concentrated gas pipeline, and the control method mainly comprises the following steps:

and (3) hot side forced exhaust pipeline adjustment: the hearth of the direct-fired incinerator is provided with a hot-side forced exhaust pipeline, one end of the hot-side forced exhaust pipeline is connected with the hearth of the direct-fired incinerator, the other end of the hot-side forced exhaust pipeline is connected with a joint between a second hot-side pipeline of the second heat exchanger and a first hot-side pipeline of the first heat exchanger, and the hot-side forced exhaust pipeline is provided with at least one air adjusting door so as to adjust the air volume of the hearth of the direct-fired incinerator through the hot-side forced exhaust pipeline.

18. An energy-saving double-runner high-concentration hot-side bypass over-temperature control method is mainly used for an organic waste gas treatment system and is provided with a direct-fired incinerator, a first heat exchanger, a second heat exchanger, a third heat exchanger, a fourth heat exchanger, a first cold-side conveying pipeline, a fourth cold-side conveying pipeline, a first adsorption rotating wheel, a second adsorption rotating wheel and a chimney, wherein the direct-fired incinerator is provided with a burner and a hearth, the burner is communicated with the hearth, the direct-fired incinerator is provided with an inlet and an outlet, the inlet is arranged at the burner, the outlet is arranged at the hearth, 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, the third heat exchanger is provided with a third cold-side pipeline and a third hot-side pipeline, the fourth heat exchanger is provided with a fourth cold-side pipeline and a fourth hot-side pipeline, one end of a 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 one end of a fourth cold-side pipeline, one end of the fourth cold-side conveying pipeline is connected with the other end of the fourth cold-side pipeline, the other end of the fourth cold-side conveying pipeline is connected with an inlet of the direct-fired incinerator, the first adsorption rotating wheel is provided with an adsorption zone, a cooling zone and a desorption zone, the first adsorption rotating wheel is connected with a waste gas inlet pipeline, a first clean gas discharge pipeline, a first cooling gas inlet pipeline, a first cooling gas conveying pipeline, a first hot gas conveying pipeline and a first desorption concentrated gas pipeline, the second adsorption rotating wheel is provided with an adsorption zone, a cooling zone and a desorption zone, and the second adsorption rotating wheel is connected with a second clean gas discharge pipeline, a second cooling gas inlet pipeline and a second cooling gas conveying pipeline, A second hot gas delivery pipeline and a second desorption concentrated gas pipeline, and the control method mainly comprises the following steps:

and (3) hot side forced exhaust pipeline adjustment: the hearth of the direct-fired incinerator is provided with a hot-side forced exhaust pipeline, one end of the hot-side forced exhaust pipeline is connected with the hearth of the direct-fired incinerator, the other end of the hot-side forced exhaust pipeline is connected with an outlet of the direct-fired incinerator, and the hot-side forced exhaust pipeline is provided with at least one air adjusting door so as to adjust the air volume of the hearth of the direct-fired incinerator through the hot-side forced exhaust pipeline.

19. The energy efficient dual-spool high-consistency hot-side bypass over-temperature control method as claimed in claim 15, 16, 17 or 18, wherein the outlet of the direct-fired incinerator is connected to the chimney.

20. The energy efficient dual spool high hot side bypass over temperature control method as claimed in claim 15, 16, 17 or 18, wherein the first cooling air intake duct is for fresh air or outside air.

21. The energy efficient dual spool high hot side bypass over temperature control method as claimed in claim 15, 16, 17 or 18, wherein the second cooling air intake duct is for fresh air or outside air.

22. The energy-saving type dual-rotor high-concentration hot-side bypass over-temperature control method as claimed in claim 15, 16, 17 or 18, wherein the exhaust gas inlet pipeline is provided with an exhaust gas communication pipeline, the exhaust gas communication pipeline is connected with the first cooling gas inlet pipeline, and the exhaust gas communication pipeline is provided with an exhaust gas communication control valve to control the air volume of the exhaust gas communication pipeline.

23. The energy-saving dual-rotor high-concentration hot-side bypass over-temperature control method as claimed in claim 15, 16, 17 or 18, wherein the first net gas discharge pipeline is provided with a first net gas communication pipeline, the first net gas communication pipeline is connected to the second cooling gas inlet pipeline, and the first net gas communication pipeline is provided with a first net gas communication control valve for controlling the air volume of the first net gas communication pipeline.

24. The energy-saving dual-rotor high-concentration hot-side bypass over-temperature control method as claimed in claim 15, 16, 17 or 18, wherein the first desorption concentrated gas pipeline is provided with a fan.

25. The energy-saving dual-rotor high-concentration hot-side bypass over-temperature control method as claimed in claim 15, 16, 17 or 18, wherein the second desorption concentrated gas pipeline is provided with a fan.

26. The energy efficient dual high-consistency hot-side bypass over-temperature control method as claimed in claim 15, 16, 17 or 18, wherein the second net gas discharge pipeline is provided with a fan.

27. The energy-saving dual-runner high-concentration hot-side bypass over-temperature control method as claimed in claim 15, 16, 17 or 18, wherein the other end of the second desorption concentrated gas pipeline in the step of delivering the second hot gas desorption is connected with the exhaust gas inlet pipeline.

28. The energy-saving dual-runner high-concentration hot-side bypass over-temperature control method as claimed in claim 15, 16, 17 or 18, wherein the other end of the second desorption concentrated gas pipeline in the step of delivering the second hot gas desorption is connected with the first cooling gas inlet pipeline.