CN103341303B - Oxidation treatment system for combustible tail gas and application thereof - Google Patents
Oxidation treatment system for combustible tail gas and application thereof Download PDFInfo
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Abstract
The invention specifically relates to an oxidation treatment system for combustible tail gas and application thereof, which belongs to the field of energy conservation and environmental protection. The oxidation treatment system comprises a primary preheater, a secondary preheater, a heat absorbing system which converts water into steam by using high temperature flue gas and an oxidation bed. According to the oxidation treatment system provided by the invention, through preheating stage by stage, a high temperature environment and high-grade heat absorption of the oxidation bed are maintained; and the primary preheater, the secondary preheater and the oxidation bed are of a partition structure, so treating capacity of the system is greatly improved.
Description
Technical field
The invention belongs to energy-conserving and environment-protective field, be specifically related to a kind of oxidization processing system and application thereof of flammable tail gas.
Background technology
Industrial production can produce a large amount of tail, waste gas.Wherein contain low-concentration combustible gas in part tail, waste gas.Such as fiery colliery ventilates weary wind, containing the methane of 0.2 ~ 1%.Because concentration is too low, this tail, waste gas cannot directly burn, normally directly emptying.This not only causes energy waste, also can bring serious environmental pollution.
About process containing tail, the waste gas of low-concentration combustible gas, international, domesticly all do correlative study.Comprise: the hot back reaction device of MEGTEC company, the weary wind oxidation unit (200620081956.x) of coal mine gas of Sheng Dong company, the coal mine ventilating gas continuous countercurrent catalytic oxidation device (201110133832.7), Multistage backheating type low-concentration gas heat reflux catalytic oxidation device (201120175395.0) etc. of University Of Science and Technology Of Hunan.These apparatus systems are all adopt ceramic heat storage body to renew fuel gas oxidation reaction heat to maintain high-temperature oxidation environment, but still there is following problem: 1, oxidation bed complex structure, ceramic heat storage body circulating resistance is comparatively large, realizes extensive gas (60,000 m
3/ more than h) process have difficulties; 2, when combustable gas concentration is too low, in order to maintain the temperature of heat storage, general stopping heat-obtaining, water-cooled heat taking and exchanging device is not now had to be chronically exposed in more than 800 DEG C even high temperature of 1200 DEG C, oxidation environment, far away higher than the bearing temperature scope of boiler steel, heat resisting steel, make heat exchanger material type selecting difficulty, especially need the pressure bearing system of production water steam; 3, when combustable gas concentration is too high, there is the possibility of superelevation in regenerator temperature, not only affects the heat storage life-span, also can affect enclosed structure support strength, cause the accident; 4, heat-obtaining quality is lower, is generally below 1.0MPa 2 steam or hot water; 5, gas needs periodically commutation in oxidation bed, affects treatment effeciency, although (201110133832.7) achieve continuous process do not need commutation, it can not heat-obtaining.6, oxidation bed structure is faviform ceramic heat retainer, and ceramic honeycomb material heat transfer property is poor, windage large, affects oxidation bed treatment effeciency; 7, adopt electrical heating start up system, this Starting mode cost is too high, especially more than 60,000 m
3the extensive treatment system of/more than h.
Summary of the invention
The invention provides a kind of oxidization processing system and application thereof of flammable tail gas, solving existing oxidation bed structure is faviform ceramic heat retainer, ceramic honeycomb material heat transfer property is poor, windage is large, affect oxidation bed treatment effeciency, ceramic heat storage body circulating resistance is comparatively large, realizes extensive gas (60,000 m
3/ more than h) process the problem and wholely provide higher to the requirement of material, the problems such as equipment investment is large, and operating cost is high such as to have difficulties.
For solving the problems of the technologies described above, the technical solution used in the present invention is:
A kind of oxidization processing system of flammable tail gas, comprise a preheater, secondary preheating device, the heat energy of high-temperature flue gas is utilized water to be converted into heat-obtaining system and the oxidation bed of steam, the inlet exhaust gas of a described preheater is provided with wind inlet channel, the offgas outlet of a described preheater is connected with the inlet exhaust gas of secondary preheating device by middle warm air road, the exhanst gas outlet of a described preheater is provided with smoke duct, the gas approach of a described preheater is connected with the exhanst gas outlet of secondary preheating device by middle temperature flue gas air channel, the offgas outlet of described secondary preheating device is connected with the high-temperature flue gas import of oxidation bed by high temperature air channel, the gas approach of described secondary preheating device to be exported with the high-temperature flue gas of oxidation bed by high-temperature flue gas air channel and is connected, the oxidation gas approach of described oxidation bed is connected with the oxidation exhanst gas outlet of oxidation bed by oxidation flue, high-temperature flue gas bypass air channel is provided with between described high-temperature flue gas air channel and described middle temperature flue gas air channel, described high-temperature flue gas bypass air channel is provided with bypass air-valve, described middle temperature flue gas air channel is provided with heat-obtaining system, described heat-obtaining system is positioned at the right of bypass air-valve, described high temperature air channel is provided with the burner that can produce high-temperature flue gas.
Further, a preferred embodiment of the present invention: described oxidation bed comprises dividing plate and potsherd, oxidation bed is separated into the oxidation bed runner of some bar shapeds by described potsherd, dividing plate is adopted to be installed together between adjacent oxidation bed runner, every sheet potsherd one effluent oxidation flue gas, one effluent high-temperature flue gas, combined crosswise.
Further, a preferred embodiment of the present invention: a described preheater and described secondary preheating device, for dividing wall structure, comprise heat-resisting steel disc, housing and preheater runner, described heat-resisting steel disc is arranged on the inside of housing, and preheater is separated into some preheater runners by heat-resisting steel disc, heat-resisting steel disc side stream tail gas, one side-stream smoke, combined crosswise.
Further, a preferred embodiment of the present invention: the cross section of described preheater runner is bar shaped, square or triangle.
Further, a preferred embodiment of the present invention: described heat-obtaining system comprises steam-water separator, attemperator, superheater and steam generator, described steam generator is arranged on middle temperature flue gas air channel, described steam generator and described steam-water separator are installed together, shown steam-water separator and described superheater are installed together, described superheater is provided with attemperator, described steam generator and shown attemperator are connected with feedwater piping, and described superheater is connected with jet chimney.
Further, a preferred embodiment of the present invention: described burner is gas burner or oil burner.
Further, a preferred embodiment of the present invention: the import of described wind inlet channel is provided with pressure fan.
Further, a preferred embodiment of the present invention: described bypass air-valve comprises housing, motor, spool, seal and roller shutter, described motor and spool are arranged in housing, described motor and described spool are linked together by belt, described roller shutter through high-temperature flue gas bypass air channel, the two ends of described roller shutter are arranged on spool, and described roller shutter and described high-temperature flue gas bypass air channel are sealed by seal.
An oxidation treatment method for flammable tail gas, comprises the following steps:
Initial start: first close bypass air-valve, start pressure fan, make to be full of tail gas in system, then burner is started, form high-temperature flue gas, by high-temperature flue gas heated oxide bed one by one, secondary preheating device, a preheater, detect oxidation bed high-temperature flue gas outlet temperature, and secondary preheating device, the offgas outlet temperature of a preheater, if oxidation bed high-temperature flue gas outlet temperature reaches 950-1050 DEG C, secondary preheating device offgas outlet temperature reaches 700-800 DEG C, No. one time preheater offgas outlet temperature reaches 280-320 DEG C, close gas burner or oil burner, start and terminate,
Normal operation: pressure fan constantly sends into the tail gas through purification of 20 ~ 35 DEG C to system, first tail gas pass through a preheater preheats to 300 ~ 350 DEG C, be preheating to more than 750 DEG C through secondary preheating device again, enter oxidation bed temperature and rise to more than 800 DEG C, carry out oxidation reaction; The high-temperature flue gas of 1000 ~ 1200 DEG C is generated after oxidation, tail gas in reflux oxidation bed preheating oxidation bed, temperature is down to 800 ~ 1000 DEG C, enters secondary preheating device pre-hot exhaust gas again, temperature is down to 400 ~ 600 DEG C, the high-temperature flue gas of 400 ~ 600 DEG C enters heat-obtaining system, and through heat-obtaining system heat-obtaining, flue-gas temperature is down to 400 DEG C, then a preheater is entered, pre-hot exhaust gas again, temperature is down to less than 80 DEG C, discharge environment;
Heat-obtaining: detect the temperature entering the flue gas of a preheater, decide heat-obtaining system and whether run, if flue-gas temperature is lower than 400 DEG C, then out of service; If higher than 500 DEG C, then put into operation, by regulating heat-obtaining system heat-obtaining amount, regulating the flue-gas temperature entering a preheater, making it to maintain about 400 DEG C, ensureing that a preheater flue gas outlet temperature is at 300 ~ 350 DEG C.
Beneficial effect of the present invention:
1, oxidation bed hot environment is maintained
Environment temperature (about 20 ~ 35 DEG C) containing the tail gas of low-concentration combustible gas, through preheater, the preheating of secondary preheating device two-stage, temperature reaches near burning-point, then enters oxidation bed.First, because warm-up phase wind-warm syndrome lower (lower than 800 DEG C), No. one time preheater, secondary preheating device adopt the heat resisting steel materials such as Cr18Ni9, and heat transfer effect is much better than pottery; Secondly, No. one time preheater, secondary preheating device adopt dividing wall structure form: preheater is separated into some bar shapeds, square or leg-of-mutton preheater runner by heat-resisting steel disc, heat-resisting steel disc side stream tail gas, a side-stream smoke, combined crosswise.Dividing wall structure can reduce the heat transfer temperature difference between tail gas and flue gas further, promotes the temperature entering oxidation bed tail gas.Through above measure, the exhaust temperature entering oxidation bed can be made to be preheated near burning-point, and tail gas significantly reduces at the caloric receptivity of oxidation bed, and the thermal discharge (calorific value) that therefore fuel gas is less can maintain oxidation bed hot environment.
2, reduce oxidation bed volume, improve the measure of oxidation bed disposal ability
First, due to tail gas enter oxidation bed close to ignition temperature, slightly heat the burning-point that can meet or exceed fuel gas through oxidation bed and complete oxidation, the heat output in oxidation bed significantly reduces.Secondly, oxidation bed adopts dividing wall structure, that is: oxidation bed is separated into the oxidation bed runner of some bar shapeds by potsherd, and every sheet potsherd one effluent tail gas, a side-stream smoke, combined crosswise, heat transfer effect and windage are better than ceramic honeycomb heat storage type.By above measure, oxidation bed volume and heat exchange area can be reduced, and realize tail gas and process continuously, improve oxidation bed operating efficiency.
3, regulate oxidation bed, secondary preheating actuator temperature too high
High-temperature flue gas air channel between oxidation bed and secondary preheating device is opened ventilating duct-high-temperature flue gas bypass air channel on one side.If oxidation high bed temperature, open bypass air-valve, by part high-temperature flue gas bypass, reduce secondary preheating device offgas outlet temperature; Because the exhaust temperature entering oxidation bed reduces, it also increases at the caloric receptivity of oxidation bed, and oxidation reinforced bed cooling, realizes oxidation bed cooling.Because secondary preheating device flue gas input reduces, the temperature of secondary preheating device also can reduce.
4, improve heat-obtaining quality
By preheater, secondary preheating device and an oxidation bed, smoke heat energy is divided into 80 ~ 400 DEG C, 400 ~ 600 DEG C, 600 ~ 1000 DEG C, 1000 ~ 1100 DEG C four temperature sections.Wherein, 80 ~ 400 DEG C of temperature sections are used for new tail gas preheating, tail gas from environment temperature to 300 ~ 350 DEG C; 600 ~ 1000 DEG C of temperature sections are used for preheating high-temperature tail gas, are preheated to 750 ~ 800 DEG C from 300 ~ 350 DEG C; 1000 ~ 1100 DEG C of temperature sections maintain oxidation bed hot environment; 400 ~ 600 DEG C of temperature sections are used for heat-obtaining.Because heat-obtaining system flue gas environment is at 400 ~ 600 DEG C, 300 DEG C, the steam of more than 4.5MPa HTHP can be obtained.
5, heat-obtaining system material problem is solved
Because a preheater requires that flue-gas temperature only has 400 DEG C, as long as so heat-obtaining system outlet flue gas can possess heat-obtaining condition higher than 400 DEG C.When the combustable gas concentration in tail gas too low cannot heat-obtaining time, the cigarette temperature entering heat-obtaining system should at about 400 DEG C.At this temperature, during the common materials such as heat-obtaining system employing boiler steel, security of operation can be ensured, there is not the over-temp and over-pressure problem of heat exchange tubing.
Accompanying drawing explanation
In order to be illustrated more clearly in the embodiment of the present invention or technical scheme of the prior art, be briefly described to the accompanying drawing used required in embodiment or description of the prior art below, apparently, accompanying drawing in the following describes is only some embodiments of the present invention, for those of ordinary skill in the art, under the prerequisite not paying creative work, other accompanying drawing can also be obtained according to these accompanying drawings.
Fig. 1 is the structural representation sketch of oxidization processing system of the present invention.
Fig. 2 is the structural representation sketch of a preheater in Fig. 1.
Fig. 3 is that the A-A of Fig. 2 is to structural representation sketch.
Fig. 4 is the structural representation sketch of the secondary preheating device in Fig. 1.
Fig. 5 is the structural representation sketch of the bypass air-valve in Fig. 1.
Fig. 6 is the structural representation sketch of the oxidation bed in Fig. 1.
Fig. 7 is the internal structure simplified schematic diagram of the oxidation bed in Fig. 6.
Note: the B-B in Fig. 4 is identical to structural representation sketch with the A-A of Fig. 2 to structural representation sketch, no longer lists.
Detailed description of the invention
Below in conjunction with the accompanying drawing in the embodiment of the present invention, be clearly and completely described the technical scheme in the embodiment of the present invention, obviously, described embodiment is only the present invention's part embodiment, instead of whole embodiments.Based on the embodiment in the present invention, those of ordinary skill in the art, not making the every other embodiment obtained under creative work prerequisite, belong to the scope of protection of the invention.
As shown in figs. 1-7, a kind of oxidization processing system of flammable tail gas, comprises preheater 2, secondary preheating device 15, heat-obtaining system and an oxidation bed 12.A preheater 2, for dividing wall structure, comprise heat-resisting steel disc 24, housing 25 and preheater runner 28, heat-resisting steel disc 24 is arranged on the inside of housing 25, preheater 2 is separated into some bar shapeds, square or leg-of-mutton preheater runner 28 by heat-resisting steel disc 24, and the present embodiment is triangle, heat-resisting steel disc 24 1 effluent tail gas, one side-stream smoke, combined crosswise.Heat-resisting steel disc 24 adopts Cr18Ni9 material.
The structure of secondary preheating device 15 is the same with the structure of a preheater 2, for dividing wall structure, comprise heat-resisting steel disc 31, housing 32 and preheater runner, heat-resisting steel disc 31 is arranged on the inside of housing 32, and it is bar shaped, square or leg-of-mutton preheater runner that preheater 15 is separated into some cross sections by heat-resisting steel disc 31, the present embodiment is triangle, heat-resisting steel disc 31 1 effluent tail gas, a side-stream smoke, combined crosswise.Heat-resisting steel disc 31 adopts Cr18Ni9 material.
Heat-obtaining system comprises steam generator 19, steam-water separator 5, attemperator 17 and superheater 18, steam generator 19 is arranged on middle temperature flue gas air channel 3, steam generator 19 is together with steam-water separator 5, steam-water separator 5 and superheater 18 are installed together, superheater 18 is provided with attemperator 17, steam generator 19 and attemperator 17 are connected with feedwater piping 4, and superheater 18 is connected with jet chimney 6.
During heat-obtaining, join inside steam generator 19 by feed pipe 6 by water, the high-temperature flue gas inside middle temperature flue gas air channel 3 is by water heating produces steam, and the heat of high-temperature flue gas is pulled away, and temperature reduces.Steam becomes dry steam under the effect of steam-water separator 5, and then under the effect of superheater 18, steam becomes high temperature, high steam, and high temperature, high steam are transported to production line by jet chimney 6.
Oxidation bed 12 comprises dividing plate 45 and potsherd 46, oxidation bed 12 is separated into the oxidation bed runner 47 of some bar shapeds by potsherd 46, adopts dividing plate 45 to be installed together between adjacent oxidation bed runner 47, every sheet potsherd 46 1 effluent oxidation flue gas, one effluent high-temperature flue gas, combined crosswise.
The inlet exhaust gas 22 of a preheater 2 is provided with wind inlet channel 20, the import of wind inlet channel 20 is provided with pressure fan 21, the offgas outlet 27 of a preheater 2 is connected with the inlet exhaust gas 29 of secondary preheating device 15 by middle warm air road 16, the exhanst gas outlet 23 of a preheater 2 is provided with smoke duct 1, and the gas approach of a preheater 2 is connected with the exhanst gas outlet 30 of secondary preheating device 15 by middle temperature flue gas air channel 3, the offgas outlet 34 of secondary preheating device 15 is connected with the high-temperature tail gas import 43 of oxidation bed 12 by high temperature air channel 14, the gas approach 33 of secondary preheating device 15 exports 41 by high-temperature flue gas air channel 11 with the high-temperature flue gas of oxidation bed 12 and is connected, the oxidation gas approach 42 of oxidation bed 12 is connected with the oxidation exhanst gas outlet 44 of oxidation bed 12 by oxidation flue 13, high-temperature flue gas bypass air channel 7 is provided with between high-temperature flue gas air channel 11 and middle temperature flue gas air channel 3, high-temperature flue gas bypass air channel 7 is provided with bypass air-valve 8, middle temperature flue gas air channel 3 is provided with the heat-obtaining system that will the heat energy water of high-temperature flue gas utilized to be converted into steam, heat-obtaining system is positioned at the right of bypass air-valve 8, high temperature air channel 14 is provided with the burner 9 that can produce high-temperature flue gas, described burner 9 is gas burner or oil burner.
Bypass air-valve 8 comprises housing 35, motor 36, spool 38, seal 39 and roller shutter 40, motor 36 and spool 38 are arranged in housing, motor 36 and spool 38 are linked together by belt 37, roller shutter 40 through high-temperature flue gas bypass air channel 7, the two ends of roller shutter 40 are arranged on spool 38, and roller shutter 40 and high-temperature flue gas bypass air channel 7 are sealed by seal 39.
Utilize oxidization processing system of the present invention, the oxidation treatment method of the flammable tail gas of process process, comprises the following steps:
Initial start:
First bypass air-valve is closed, start pressure fan, make to be full of tail gas in system, then burner is started, form high-temperature flue gas, by high-temperature flue gas heated oxide bed one by one, secondary preheating device, a preheater, detect oxidation bed high-temperature flue gas outlet temperature, and secondary preheating device, the offgas outlet temperature of a preheater, if oxidation bed high-temperature flue gas outlet temperature reaches 950-1050 DEG C, secondary preheating device offgas outlet temperature reaches 700-800 DEG C, No. one time preheater offgas outlet temperature reaches 280-320 DEG C, close gas burner or oil burner, start and terminate,
Normal operation:
Pressure fan constantly sends into the tail gas through purification of 20 ~ 35 DEG C to system, first tail gas pass through a preheater preheats to 300 ~ 350 DEG C, then be preheating to more than 750 DEG C through secondary preheating device, enters oxidation bed temperature and rise to more than 800 DEG C, carry out oxidation reaction; The high-temperature flue gas of 1000 ~ 1200 DEG C is generated after oxidation, tail gas in reflux oxidation bed preheating oxidation bed, temperature is down to 800 ~ 1000 DEG C, enters secondary preheating device pre-hot exhaust gas again, temperature is down to 400 ~ 600 DEG C, the high-temperature flue gas of 400 ~ 600 DEG C enters heat-obtaining system, and through heat-obtaining system heat-obtaining, flue-gas temperature is down to 400 DEG C, then a preheater is entered, pre-hot exhaust gas again, temperature is down to less than 80 DEG C, discharge environment;
Heat-obtaining:
Detect the temperature entering the flue gas of a preheater, decide heat-obtaining system and whether run, if flue-gas temperature is lower than 400 DEG C, then out of service; If higher than 500 DEG C, then put into operation, by regulating heat-obtaining system heat-obtaining amount, regulating the flue-gas temperature entering a preheater 2, making it to maintain about 400 DEG C, ensureing that a preheater 2 offgas outlet temperature is at 300 ~ 350 DEG C.
Oxidation bed temperature adjustment process:
Detect oxidation bed oxidation flue temperature, if higher than 1200 DEG C, then oxidation high bed temperature is described, open bypass air-valve, by-passing part flue gas, reduce the high-temperature flue gas outlet temperature of secondary preheating device, increase tail gas to recept the caloric at oxidation bed, oxidation bed is cooled; If temperature is lower than 850 DEG C, illustrate that oxidation bed temperature is too low, start burner, carry out afterburning.
Secondary preheating actuator temperature adjustment process:
Detect the high-temperature tail gas outlet temperature of secondary preheating device, if higher than 800 DEG C, then illustrate that secondary preheating actuator temperature is too high, opens bypass air-valve, by-passing part flue gas, reduce secondary preheating device flue gas input, secondary preheating device is lowered the temperature.
Stopping process:
If detect burner in operation, then close down burner; If it is out of service to detect heat-obtaining system, then starts, and be adjusted to full load state; Open bypass air-valve completely, by pass flue; Detect the temperature of oxidation flue, if lower than 800 DEG C, close down pressure fan, system is out of service.
The foregoing is only preferred embodiment of the present invention, not in order to limit the present invention, within the spirit and principles in the present invention all, any amendment done, equivalent replacement, improvement etc., all should be included within protection scope of the present invention.
Claims (8)
1. the oxidation treatment method of a flammable tail gas, it is characterized in that: comprise a preheater, secondary preheating device, the heat energy of high-temperature flue gas is utilized water to be converted into heat-obtaining system and the oxidation bed of steam, the inlet exhaust gas of a described preheater is provided with wind inlet channel, the offgas outlet of a described preheater is connected with the inlet exhaust gas of secondary preheating device by middle warm air road, the exhanst gas outlet of a described preheater is provided with smoke duct, the gas approach of a described preheater is connected with the exhanst gas outlet of secondary preheating device by middle temperature flue gas air channel, the offgas outlet of described secondary preheating device is connected with the high-temperature flue gas import of oxidation bed by high temperature air channel, the gas approach of described secondary preheating device to be exported with the high-temperature flue gas of oxidation bed by high-temperature flue gas air channel and is connected, the oxidation gas approach of described oxidation bed is connected with the oxidation exhanst gas outlet of oxidation bed by oxidation flue, high-temperature flue gas bypass air channel is provided with between described high-temperature flue gas air channel and described middle temperature flue gas air channel, described high-temperature flue gas bypass air channel is provided with bypass air-valve, described middle temperature flue gas air channel is provided with heat-obtaining system, described heat-obtaining system is positioned at the right of bypass air-valve, described high temperature air channel is provided with the burner that can produce high-temperature flue gas,
Comprise the following steps:
Initial start: first close bypass air-valve, start pressure fan, make to be full of tail gas in system, then burner is started, form high-temperature flue gas, by high-temperature flue gas heated oxide bed one by one, secondary preheating device, a preheater, detect oxidation bed high-temperature flue gas outlet temperature, and secondary preheating device, the offgas outlet temperature of a preheater, if oxidation bed high-temperature flue gas outlet temperature reaches 950-1050 DEG C, secondary preheating device offgas outlet temperature reaches 750-800 DEG C, No. one time preheater offgas outlet temperature reaches 280-320 DEG C, close gas burner or oil burner, start and terminate,
Normal operation: pressure fan constantly sends into the tail gas through purification of 20 ~ 35 DEG C to system, first tail gas pass through a preheater preheats to 300 ~ 350 DEG C, be preheating to more than 750 DEG C through secondary preheating device again, enter oxidation bed temperature and rise to more than 800 DEG C, carry out oxidation reaction; The high-temperature flue gas of 1000 ~ 1200 DEG C is generated after oxidation, tail gas in reflux oxidation bed preheating oxidation bed, temperature is down to 800 ~ 1000 DEG C, enters secondary preheating device pre-hot exhaust gas again, temperature is down to 400 ~ 600 DEG C, the high-temperature flue gas of 400 ~ 600 DEG C enters heat-obtaining system, and through heat-obtaining system heat-obtaining, flue-gas temperature is down to 400 DEG C, then a preheater is entered, pre-hot exhaust gas again, temperature is down to less than 80 DEG C, discharge environment;
Heat-obtaining: detect the temperature entering the flue gas of a preheater, decide heat-obtaining system and whether run, if flue-gas temperature is lower than 400 DEG C, then out of service; If higher than 500 DEG C, then put into operation, by regulating heat-obtaining system heat-obtaining amount, regulating the flue-gas temperature entering a preheater, making it to maintain about 400 DEG C, ensureing that a preheater flue gas outlet temperature is at 300 ~ 350 DEG C.
2. the oxidation treatment method of a kind of flammable tail gas according to claim 1, it is characterized in that: described oxidation bed comprises dividing plate and potsherd, oxidation bed is separated into the oxidation bed runner of some bar shapeds by described potsherd, dividing plate is adopted to be installed together between adjacent oxidation bed runner, every sheet potsherd one effluent oxidation flue gas, one effluent high-temperature flue gas, combined crosswise.
3. the oxidation treatment method of a kind of flammable tail gas according to claim 1, it is characterized in that: a described preheater and described secondary preheating device, for dividing wall structure, comprise heat-resisting steel disc, housing and preheater runner, described heat-resisting steel disc is arranged on the inside of housing, and preheater is separated into some preheater runners by heat-resisting steel disc, heat-resisting steel disc side stream tail gas, one side-stream smoke, combined crosswise.
4. the oxidation treatment method of a kind of flammable tail gas according to claim 3, is characterized in that: the cross section of described preheater runner is bar shaped, square or triangle.
5. the oxidation treatment method of a kind of flammable tail gas according to claim 1, it is characterized in that: described heat-obtaining system comprises steam-water separator, attemperator, superheater and steam generator, described steam generator is arranged on middle temperature flue gas air channel, described steam generator and described steam-water separator are installed together, described steam-water separator and described superheater are installed together, described superheater is provided with attemperator, described steam generator and shown attemperator are connected with feedwater piping, and described superheater is connected with jet chimney.
6. the oxidation treatment method of a kind of flammable tail gas according to claim 1, is characterized in that: described burner is gas burner or oil burner.
7. the oxidation treatment method of a kind of flammable tail gas according to claim 1, is characterized in that: the import of described wind inlet channel is provided with pressure fan.
8. the oxidation treatment method of a kind of flammable tail gas according to claim 1, it is characterized in that: described bypass air-valve comprises housing, motor, spool, seal and roller shutter, described motor and spool are arranged in housing, described motor and described spool are linked together by belt, described roller shutter through high-temperature flue gas bypass air channel, the two ends of described roller shutter are arranged on spool, and described roller shutter and described high-temperature flue gas bypass air channel are sealed by seal.
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