CN108926996A - A kind of cyclone type coal mine methane catalyst oxidation reactor - Google Patents
A kind of cyclone type coal mine methane catalyst oxidation reactor Download PDFInfo
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- CN108926996A CN108926996A CN201810837037.8A CN201810837037A CN108926996A CN 108926996 A CN108926996 A CN 108926996A CN 201810837037 A CN201810837037 A CN 201810837037A CN 108926996 A CN108926996 A CN 108926996A
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Abstract
A kind of cyclone type coal mine methane catalyst oxidation reactor belongs to super low concentration Catalytic methane oxidation technical field.It include: inlet and exhaust system, pre-heating system, reaction system, pipe-line system and TT&C system.After idle air is preheated in preheater, entered in first reactor with the tangential mode of entrance of spiral case, when gas rotates from top to bottom along reactor wall, is reacted with the catalyst being coated on reactor wall, generate CO2And H2O, simultaneously, grit in idle air falls into ash bucket along reactor wall and is purified, high-temperature gas after reaction is rotated along axle center upwards again, it is most escaped and enter in second reactor through exhaust pipe afterwards, gas occurs similarly to react in the second reactor, and discharges a large amount of heat, toward complex Alternating, maintaining certainly for device is realized.The present invention can handle concentration in the idle air of 0.1%-5%, and maximum throughput is up to 1000m3/ h, gas flow rate reach as high as 1000 DEG C up to 0.35m/s, the operating temperature of the reactor, and removal rate reaches 80% or more.
Description
The application be the applying date be on 08 10th, 2015, application No. is 201510488057.5, entitled one kind
The divisional application of cyclone type coal mine methane catalyst oxidation reactor.
Technical field
The present invention relates to a kind of cyclone type coal mine methane catalytic oxidation reaction devices, belong to super low concentration methane oxidation technology
Field.
Background technique
Coal mine methane is one of main gas industrial emission source, currently, the whole world is discharged into atmosphere because of coal mining every year
In CH4Total amount is 25,000,000 t, wherein 70% (China is 90%) comes from coal mine methane (VAM).Methane is to be only second to titanium dioxide
The important greenhouse gases of carbon, influence of the methane of unit mass to atmospheric warming effect are equivalent to the 21 of homogenous quantities carbon dioxide
Times, by CH4It is directly discharged in atmosphere, not only causes the serious waste of limited non-renewable resources, but also exacerbate temperature
Room effect, causes atmosphere pollution.Due to assigning for country policy and energy-saving tasks clear index greatly, national coal mining enterprise face
Face energy-saving immense pressure, the utilization of coal mine methane becomes particularly important.Coal mine methane discharge capacity is big, gas density it is low with
And concentration is unstable, these features determine that coal mine wind-lack gas is difficult with conventional burners and is not having the case where auxiliary fuel
It directly burns down.Currently, hot counter-current catalytic oxidation technology (Catalytic Flow-Reversal Reactor, CFRR)
It is one of the major technique for realizing the effective recycling of coal mine methane low-concentration methane.
CFRR can make methane carry out low-temperature oxidation in catalyst surface, its working principle is that, device is carried out first pre-
Heat (electric heating or conveys high-temperature flue gas by burner, control valve is opened after the completion of preheating, the coal mine methane entrance under room temperature
Device and in the flowing direction constantly heating, temperature reaches autoignition conditions and starts to aoxidize when reaching middle part catalyst area, reacts
High-temperature gas afterwards continues to flow, and to the heat-accumulating area of outlet side, the heat-accumulating area temperature of outlet side can be increased constantly for continuous heat release, together
When the room temperature VAM that is passed into of inlet heat-accumulating area gradually cool down, switching control valve after a period of time, the flow direction of coal mine methane
Change, constantly repeatedly above procedure, it is no longer necessary to which additional input heat can spontaneous maintenance operation.React generate heat in addition to
It maintains to be extracted except self-operating and generate steam or hot water, for generating electricity or heat supply.
Currently, being only limitted to laboratory stage to the application of CFRR technology both at home and abroad, by consulting literatures, summarize at present
CFRR device still needs to solve the problems, such as: (1) how realization device from maintain；(2) oxidation bed of CFRR is made pottery by a large amount of honeycomb
The problems such as porcelain is constituted, and cracking, broken and blocking can occur after long-term use for ceramic honey comb, needs timing to replace, maintenance cost is high；
(3) single reactor makes the residence time of gas too short, insufficient so as to cause gas reaction；(4) contain in coal mine methane
There is a large amount of dust, if not being dusted purification to gas, catalyst can not only be polluted, reduces catalyst activity,
It also will affect the atmospheric environment of surrounding.
Summary of the invention
It is an object of the invention in view of the defects existing in the prior art, provide a kind of cyclone type coal mine methane catalysis oxidation
Device, it solves the problems such as existing mine air-lack is directly discharged to energy waste present in atmosphere and environmental pollution, and reaches
To the effect of resource utilization.Its technical solution are as follows:
A kind of cyclone type coal mine methane catalytic oxidizing equipment, including into exhaust system, pre-heating system, reaction system, pipe-line system
And TT&C system.It is characterized by:
Gas handling system includes air inlet pipe and air inlet diffuser, and exhaust system includes escape pipe, outlet reducing pipe and air-introduced machine.Outlet
It is extracted by air-introduced machine.Air inlet diffuser passes through preheater insulating layer and connect with preheater, and outlet diffuser passes through preheater
Insulating layer is connect with preheater.
Pre-heating system includes that preheater, insulating layer, air inlet diffuser, the first idle air outlet, exhaust gas entrance, the second idle air go out
Mouth, waste gas outlet composition.Idle air entrance, the outlet of the first idle air, the outlet of the second idle air and exhaust gas entrance all pass through preheater heat preservation
Layer is connect with preheater.Preheater by electrically heated rod, tubular heat exchanger and gas control valve group at.Preheater is by electrically heated rod
It is heated, idle air enters preheater, is preheated by tubular heat exchanger.It is first stage, weary by first after heated
Wind outlet enters in reactor assembly, and second stage, idle air enters in reaction system through the outlet of the second idle air, after reaction
Exhaust gas all enters preheater by waste gas outlet, finally, the exhaust gas through heat exchange cooling is discharged into atmosphere by waste gas outlet.
Reaction system is composed in series by first reactor and second reactor.The structure of first reactor and second reactor
It is identical, it is made of air inlet, gas distribution grid, shell, vacuum interlayer, catalyst, cylindrical body, cone, storage ash bucket and gas outlet.
Preheat idle air after gas distribution grid, entered in reactor with the tangential entry type of spiral case, gas along reactor wall on to
Under rotate, and be coated in reactor wall on catalyst reacted, generate CO2And H2O, and discharge a large amount of
Heat.Meanwhile the grit in idle air gradually shifts to the inner wall of reactor under the action of the centrifugal force, reaches the grit on inner wall in air-flow
Ash bucket is fallen into along wall surface under gravity collective effect.After gas after reaction reaches cone base, then rotated upwards along axle center,
It is discharged through exhaust pipe from reactor head.It is vacuum interlayer between shell of reactor and catalyst, prevents scattering and disappearing for heat, play
The effect of heat preservation.
Pipe-line system is by the first idle air air inlet pipe, the first idle air escape pipe, the second idle air air inlet pipe, the second idle air outlet
Pipe, the first solenoid valve, second solenoid valve, third solenoid valve, the 4th solenoid valve and the 5th solenoid valve block at.Each solenoid valve connection
3 pipelines, control the flow direction of gas.
TT&C system include the first temperature sensor in air inlet pipe, first pressure sensor, the first concentration sensor and
Flowmeter is respectively used to temperature, pressure, concentration and the flow of measurement air inlet；The second temperature being mounted in the first idle air air inlet pipe
Sensor is spent, for measuring the flue-gas temperature for entering first reactor；Be mounted on third temperature sensor in first reactor,
4th temperature sensor, the 5th temperature sensor, for measuring the gas in reaction in the temperature of reactor different location；Installation
Second pressure sensor, the 6th temperature sensor and the second concentration sensor on the first idle air escape pipe, for measuring the
Pressure, temperature and the methane content of one reactor outlet can calculate conversion ratio of the methane after first reactor；Installation
The 7th temperature sensor in second reactor air inlet pipe, for measuring the temperature for entering the gas of second reactor；Installation
The 8th temperature sensor, the 9th temperature sensor, the tenth temperature sensor in second reactor, for measuring gas
The temperature of two reactor different locations；Third concentration sensor, the third pressure sensor being mounted on the second idle air escape pipe
And the 11st temperature sensor, for measuring the methane concentration and gas pressure and methane content that second reactor is worked off one's feeling vent one's spleen；Peace
The 12nd temperature sensor on escape pipe measures the temperature for the exhaust gas being discharged into atmosphere.Described first, second,
Third pressure sensor, first, second, third, fourth, the 5th, the 6th, the 7th, the 8th, the 9th, the ten, the first, the 12nd
The output end of temperature sensor, the first, second, third concentration sensor and flowmeter is connected by signal wire with measurement and control unit,
The control terminal of regulating valve is connected by signal wire with measurement and control unit.
The cyclone type coal mine methane catalyst oxidation reactor, reaction chamber is by air inlet pipe, cylinder, cone and exhaust pipe group
At.It is vacuum interlayer between shell of reactor and catalyst, prevents scattering and disappearing for heat, play the role of heat preservation to reactor.Instead
Device is answered to be made of high temperature resistant stainless steel, inner wall applies wear-resistant coating, not only can be with high temperature resistant, but also can reduce grit to the mill of reactor
Damage.Catalyst is applied directly to reactor wall, without the use of carriers such as ceramic honey combs, reduces the load-bearing of reactor, is dropped
The cost of manufacture and difficulty of processing of low reactor, so as to avoid because blocking and regularly replacing ceramic honey comb bring maintenance expense
With.Inside reactor movement-less part or transmission mechanism are low convenient for management, maintenance cost.Reactor be it is vertical, by bracket branch
Support.
The cyclone type coal mine methane catalyst oxidation reactor, intake method is the tangential entry type of spiral case, in air inlet pipe
Wall is tangent with cylinder, and outer wall uses involute in form, and involuted angle is 180 °.Scroll casing type entry form is easy to increase inlet -duct area,
Entrance has an annulus, keeps air inlet closer away from cylinder body outer wall, is conducive to the contact area for increasing gas and catalyst, also
Conducive to the separation of particle.In addition, scroll casing type air inlet also reduces interfering with each other for inlet air flow and inside vortex air-flow, make inlet pressure
Drop reduce, direct-insert inlet tube design with it is easily manufactured, and performance stabilization.
The cyclone type coal mine methane catalyst oxidation reactor, the first idle air air inlet pipe, the first idle air escape pipe, second
Idle air air inlet pipe, the second idle air escape pipe and the first solenoid valve, second solenoid valve, third solenoid valve, the 4th solenoid valve and the 5th
Solenoid valve is connected with each other.Each solenoid valve is connected to 3 pipelines, controls the flow direction of gas.First stage, idle air is through
The first, second, third, fourth, the 5th solenoid valve is passed sequentially through after one air inlet pipe, is finally entered by the second idle air escape pipe pre-
Hot device；Second stage, idle air pass sequentially through third, the four, the first, second, the 5th solenoid valve through the second idle air air inlet pipe,
Preheater is finally entered by the second idle air escape pipe.It is acted on simultaneously by 5 solenoid valves, can effectively control the air inlet of gas
Direction and flow direction and adjusting switching time in reactor, so that realization device maintains certainly.
The cyclone type coal mine methane catalyst oxidation reactor, first reactor and second reactor series connection, idle air warp
After preheating, it is introduced into first reactor, is entering second reactor, is increasing residence time of the idle air in reactor, increasing
The contact area of idle air and catalyst, and then the clean-up effect of idle air is improved, it further reduced the discharge worked off one's feeling vent one's spleen dense
Degree.
The cyclone type coal mine methane catalyst oxidation reactor, reaction outlet cool down back to preheater, this portion
Divide heat that will be used to heat fresh cold conditions idle air, realizes the recycling of heat, the gas through cooling down is discharged into atmosphere.
Its working principle is that: the first stage first heats preheater, and after reaching certain temperature, idle air enters pre-
Hot device is preheated, and the gas after preheating is entered in first reactor by air inlet pipe, and with coated in first reactor
The catalyst of wall is reacted, and CO is generated2And H2O, and a large amount of heat is generated, meanwhile, the grit in gas falls into ash bucket along wall
In, the gas after reaction escapes and enter second reactor by the escape pipe of reactor, and gas carries out with catalyst anti-again
It answers；Gas after reaction carries out heat exchange cooling back to preheater, this partial heat will be used to heat fresh idle air, after cooling
Gas be directly discharged in atmosphere；Second stage stops heating preheater, after fresh idle air enters preheater, by first
The heat that elementary reaction is released preheats idle air, and the gas after preheating is introduced into second reactor, and it is anti-to enter back into first
Device is answered, is finally discharged after preheater exchanges heat.So alternately, the automatic holding reaction of realization device.
Compared with prior art, the present invention its advantage is that:
1. cyclone type catalyst oxidation reactor takes full advantage of the inside and outside vortex of air-flow, can effectively increase low-concentration methane gas
Residence time in reactor increases the time of contact with catalyst, improves reaction efficiency, while can be effective using centrifugal force
Dust content in low-concentration methane is reduced, catalyst service life is extended, the gas after making reaction becomes cleaner.
2. the contact area of gas and catalyst is increased, reacts idle air sufficiently using two reactor series connection,
The efficiency for improving methane catalytic combustion, enables methane adequately to burn, and discharges more heats.The reactor can handle
Concentration is in the idle air gas of 0.1%-5%, and maximum throughput is up to 1000m3/ h, gas flow rate up to 0.35m/s, the reactor
Operating temperature reaches as high as 1000 DEG C, and treatment effeciency can achieve 80% or more.
3. not using ceramic supported catalysts in reactor, but catalyst is applied directly on reactor wall, no
The cost that reactor can only be reduced, can also reduce difficulty of processing, so as to avoid because blocking and regularly replacing ceramic honey comb
Bring maintenance cost.
4. the gas after reaction again returns to preheater and exchanges heat, the utilization rate of heat is improved, device maintains certainly
Operation, saves power consumption cost.
Fig. 1 is the process flow chart that the present invention is implemented.
Fig. 2 is the top view of reactor cross section figure shown in FIG. 1 and import.
Fig. 3 is internal structure and the gas flow figure of reactor shown in FIG. 1.
Fig. 4 is reactor pipeline design drawing shown in FIG. 1.
Fig. 5 is the methane conversion of concentration 0.8%.
Heat accumulating sections temperature change when Fig. 6 is the methane reaction of concentration 0.8%.
Fig. 7 is the temperature change of each temperature measuring point of the methane reaction different time of concentration 0.8%.
Fig. 8 is the methane conversion of concentration 0.3%.
Fig. 9 is the temperature change of each temperature measuring point of the methane reaction different time of concentration 0.3%.
Figure 10 is the methane of concentration 0.7%, the conversion ratio under different flow.
In Fig. 1: 1. air-introduced machine, 2. escape pipe, 3. preheater, 4. insulating layer, 5. air inlet diffuser, 6. air inlet pipe
7. 8. 9. first temperature sensor of first pressure sensor of the first temperature sensor, 10. flowmeter 11. first
Idle air exports 12. first 13. first solenoid valve of idle air air inlet pipe, 14. gas distribution grid, 15. second temperature and passes
16. second pressure sensor 17. of sensor, 18. second concentration sensors 19. first of the 6th temperature sensor are weary
The 5th temperature of 20. first reactor of wind escape pipe, 21. the 4th temperature sensor 23. of third temperature sensor 22.
27. vacuum interlayer of the 7th temperature sensor 25. air inlet, 26. shell of sensor 24., 28. catalyst
29. 30. cone 31. of cylindrical body stores up the 8th temperature sensor 34. of 32. second reactor 33. of ash bucket the
37. third concentration sensor 38. of the tenth 36. second idle air escape pipe of temperature sensor of nine temperature sensors 35.
40. measurement and control unit of third the 11st temperature sensor of pressure sensor 39., 41. third solenoid valve 42. second
47. exhaust gas entrance 48. the tenth of the 4th 45. second the 5th solenoid valve of air inlet pipe 46. of solenoid valve of solenoid valve 43.
Two temperature sensors, 49. second idle air exports 50. waste gas outlets
In Fig. 2: 25. air inlet, 29. cylindrical body, 30. cone 31. stores up 51. scroll casing type air inlet pipe 52. first of ash bucket
53. gas outlet of flange, 54. upper bracket, 55. support, 56. second flange, 57. support plate, 58. lower bracket
In Fig. 3: 4. insulating layer, 25. air inlet, 26. shell, 27. vacuum interlayer, 28. catalyst, 29. cylindrical body
It is vortexed outside 53. gas outlet of ash bucket, 59. inside vortex 60. 30. cone 31. is stored up
In Fig. 4: the 4th solenoid valve 46. of 13. first solenoid valve, 41. third solenoid valve, 42. second solenoid valve 43.
Five solenoid valves.
Specific embodiment
Embodiment of the present invention is further illustrated below with reference to embodiment.
Embodiment 1
As shown in Fig. 2, idle air is entered in reactor with the tangential entry type of spiral case, air inlet inside pipe wall is tangent with cylinder, and outer wall is adopted
With involute in form, involuted angle is 180 °.Reactor shell is by air inlet, scroll casing type air inlet pipe, cylindrical body, cone, storage ash bucket
It is formed with gas outlet.Air inlet is arranged on the cylinder, and by flanged joint, reactor is supported by bracket and support plate, bracket
It is connected with pedestal, keeps reactor more firm.
As shown in figure 3, flow direction of the gas in reactor is broadly divided into outer vortex and inside vortex.Gas enters reaction
After device, rotate from top to bottom along reactor outer wall, i.e., it is outer to be vortexed.At this point, gas with coated on reactor wall
Catalyst is reacted, meanwhile, the grit contained in gas gradually shifts to the inner wall of reactor under the action of the centrifugal force, in arrival
Grit on wall falls into ash bucket along wall surface under air-flow and gravity collective effect.After gas after reaction reaches cone base, turn
And rotated upwards along axle center, i.e., inside vortex, last gas are discharged through exhaust pipe from reactor head.In being vortexed outside downwards and being upward
The airflow direction of vortex is opposite.It is vacuum interlayer between shell of reactor and catalyst, prevents scattering and disappearing for heat, play guarantor
The effect of temperature.
As shown in figure 4, black arrows represent the flow direction of first stage gas, hollow arrow represents second stage gas
Flow direction, dotted line represents the pipeline of first stage, and solid line represents the pipeline of second stage.First stage, gas enter preheater
Afterwards, along dotted line pipeline, enter first reactor by the first solenoid valve, after reaction, outlet successively pass through second solenoid valve,
Third solenoid valve enters second reactor, and after reaction, exhaust gas is successively again introduced into preheating through the 4th solenoid valve, the 5th solenoid valve
Device heat exchange, is finally discharged into atmosphere；Second stage, after gas enters preheater, by solid line pipeline, by third solenoid valve
It enters in second reactor, outlet successively passes through the 4th solenoid valve, the first solenoid valve enters in first reactor, after reaction
Gas successively enter preheater through second solenoid valve, third solenoid valve, be finally discharged into atmosphere, with this realization device
From maintenance.
As shown in Figure 1, the course of work of the device is as follows:
First reactor and second reactor are preheated first, after reaching preheating temperature, unlatching first, second, third,
Four, the 5th solenoid valves, fresh idle air, which passes through air inlet pipe 6 first and enters in preheater 3, to be preheated, by the gas of preheating
Body enters in first reactor through gas outlet 11, the first solenoid valve 13.At this point, gas will be along reactor wall with spiral side
Formula rotates from top to bottom, and is reacted with coated in the catalyst on reactor wall, and CO is generated2And H2O, and release
The heat of amplification quantity, at the same time, the grit contained in gas gradually shift to the inner wall of reactor under the action of the centrifugal force, in arrival
Grit on wall falls into ash bucket along wall surface under air-flow and gravity collective effect.After gas after reaction reaches cone base, turn
And upwards along axle center rotate, and via the first idle air escape pipe 19, second solenoid valve 42, third solenoid valve 41 and air inlet 25 into
Enter into second reactor, the heat that gas carries is for heating second reactor.Gas occurs equally in the second reactor
Reaction, the gas after reaction enters in preheater via the 4th solenoid valve 43 and the 5th solenoid valve 46 carries out heat recovery,
A part of heat is for heating fresh idle air, and another part recycling is for resident's heating etc., finally, work of the gas in air-introduced machine
It is discharged into atmosphere under by escape pipe 2.Second stage, switching solenoid valve, fresh idle air air inlet pipe 6 of leaving enter preheating
In device, the gas after preheating enters in second reactor through the second idle air outlet 49, third solenoid valve 41, air inlet 25, this
When gas first react in the second reactor, the high-temperature gas after reaction is through the 4th solenoid valve 43,13 and of the first solenoid valve
Gas distribution grid 14 enters in first reactor, and the heat that gas carries can heat first reactor again, after reacting,
High-temperature gas enters in preheater through the first idle air exhaust pipe 19, second solenoid valve 42, the 5th solenoid valve 46, is finally discharged into
In atmosphere.So on circulate, the heat generated after gas reaction can continuous heating response device, along with the work of vacuum heat-insulating layer
With so that heat loss is seldom, so that first reactor and second reactor are still in the case where not needing external heat source
It can be in the condition of high temperature that gas can react, persistently with maintaining certainly for realization device.
The catalyst that the present apparatus uses is precious metals pd, with γ-Al2O3For carrier, Pd is main active.Maximum
Reason amount is 1000m3/ h is capable of handling the idle air of concentration 0.1%-5%, gas flow rate 0-0.35m/s, and treatment effeciency reaches
80% or more.The operating temperature of the reactor reaches as high as 1000 DEG C, and temperature of working off one's feeling vent one's spleen is at 60 DEG C or less.Gas flow is
1.2m3/ h, methane concentration 0.8%, commutation cycle 5min, when preheating temperature is 500 DEG C, methane conversion reaches 85% or more
(Fig. 5), heat accumulating sections temperature is in cyclically-varying (Fig. 6) with switching time, and outlet temperature is only 35 DEG C (Fig. 7), methane concentration
When being 0.3%, methane conversion remains to reach 80% or more (Fig. 8), and temperature of working off one's feeling vent one's spleen is at 45 DEG C or less (Fig. 9).
When not adding catalyst, reactor is preheating to 900 DEG C, methane concentration 0.7%, commutation cycle 10min,
With different flow air inlets, the conversion ratio of methane can reach 90% or more (Figure 10).
Embodiment 2
Reactor is preheating to 500 DEG C, gas flow 1.2m3/ h, flow velocity 0.04m/s, methane concentration 0.8%, commutation week
Phase 5min, methane conversion can reach 85% or more, and outlet temperature is only 35 DEG C.
Embodiment 3
Reactor is preheating to 500 DEG C, gas flow is 1.2 m3/ h, flow velocity 0.04m/s, methane concentration 0.3%, commutation
Period 5min, methane conversion is up to 80% or more, and temperature of working off one's feeling vent one's spleen is at 45 DEG C or less.
Embodiment 4
Catalyst is not added, reactor is preheating to 900 DEG C, methane concentration 0.7%, commutation cycle 10min, charge flow rate
Respectively 1.2 m3/h、1.4 m3/h、1.6 m3When/h, the conversion ratio of methane is up to 90% or more.
Embodiment 5
Reactor is preheating to 500 DEG C, gas flow 10m3/ h, flow velocity 0.04m/s, methane concentration 0.5%, commutation week
Phase 5min, methane conversion is up to 80% or more, and temperature of working off one's feeling vent one's spleen is at 45 DEG C or less.
Embodiment 6
Catalyst is not added, reactor is preheating to 1000 DEG C or more, methane concentration 0.5%, commutation cycle 10min, air inlet
Flow is 10m3When/h, the conversion ratio of methane is up to 90% or more.
Embodiment 7
Reactor is preheating to 500 DEG C, gas flow is 1000 m3/ h, flow velocity 0.04m/s, methane concentration 1%, commutation week
Phase 5min, methane conversion is up to 60% or more, and temperature of working off one's feeling vent one's spleen is at 45 DEG C or less.
Embodiment 8
Catalyst is not added, reactor is preheating to 1000 DEG C, methane concentration 1%, commutation cycle 10min, charge flow rate is
1000m3When/h, the conversion ratio of methane is up to 65% or more.
Claims (10)
1. cyclone type catalyst oxidation reactor, it is characterised in that: the reactor includes scroll casing type air inlet pipe (51), cylinder and goes out
Port (53), scroll casing type air inlet pipe (51) inner wall and the cylinder are tangent, and outer wall uses involute in form, and involuted angle is
180°；The cylinder includes cylindrical body (29) and the centrum (30) of vertical setting；The cylinder successively includes shell from outside to inside
(26) and catalyst coat (28)；The shell (26) is provided with vacuum interlayer (27) between shell and inner wall；The catalyst
Coating (28) is applied to the shell (26) inner wall.
2. cyclone type catalyst oxidation reactor according to claim 1, it is characterised in that: the reactor further includes storage ash
It struggles against (31), storage ash bucket (31) setting is below the centrum (30).
3. cyclone type catalyst oxidation reactor according to claim 1, it is characterised in that: shell (26) inner wall also applies
It is wiped with wear-resistant coating, the wear-resistant coating is between the catalyst coat (28) and inner wall.
4. cyclone type catalyst oxidation reactor according to claim 1, it is characterised in that: the catalyst coat (28) applies
The catalyst smeared selects Pd catalyst, and the Pd catalyst is with γ-Al2O3It is main active for carrier, Pd.
5. cyclone type catalyst oxidation reactor according to claim 1, it is characterised in that: the reactor material is selected resistance to
High temperature stainless steel.
6. a kind of coal mine methane catalytic oxidizing equipment, described device can be connect with coal mine methane system, described device include into
Gas system, exhaust system, preheater (3) and reaction system, it is characterised in that:
The gas handling system is separately connected the coal mine methane system and the preheater (3)；
The reaction system includes two cyclone type catalyst oxidation reactors being connected in series, and is first reactor (20) and second
Reactor (32)；The first reactor (20) and second reactor (32) include scroll casing type air inlet pipe (51), cylinder and go out
Port (53), scroll casing type air inlet pipe (51) inner wall and the cylinder are tangent, and outer wall uses involute in form, and involuted angle is
180°；The cylinder includes cylindrical body (29) and the centrum (30) of vertical setting；The cylinder successively includes shell from outside to inside
(26) and catalyst coat (28)；The shell (26) is provided with vacuum interlayer (27) between shell and inner wall；The catalyst
Coating (28) is applied to the shell (26) inner wall；
The preheater (3) be provided with the first idle air outlet (11) and the second idle air export (49) respectively with the first reactor
(20) it is connected with second reactor (32)；The preheater (3) is additionally provided with exhaust gas entrance (47) and reacts respectively with described first
Device (20) is connected with second reactor (32)；
The preheater (3) is provided with waste gas outlet (50) and is connected with the exhaust system.
7. a kind of coal mine methane catalytic oxidizing equipment according to claim 6, it is characterised in that: the gas handling system includes
Air inlet pipe (6) and air inlet diffuser (5), the air inlet pipe (6) is for connecting coal mine methane system and the preheater (3), institute
It states and is connected between air inlet pipe (6) and the preheater (3) by air inlet diffuser (5)；The exhaust system includes escape pipe (2)
With air-introduced machine (1), the escape pipe (2) is connected with waste gas outlet (50).
8. a kind of coal mine methane catalytic oxidizing equipment according to claim 6, it is characterised in that: the preheater (3)
First idle air exports (11) and is connected with the first reactor (20) by the way that the first idle air air inlet pipe (12) is arranged, and described first is anti-
Device (20) are answered to give up respectively with the second reactor (32) and the preheater (3) by setting the first idle air escape pipe (19)
Gas entrance (47) is connected；The second reactor (32) passes through the second idle air escape pipe (36) of setting and the preheater (3)
Exhaust gas entrance (47) is connected；Pass through between the second idle air outlet (49) of the preheater (3) and the second reactor (32)
The second air inlet pipe (45) are arranged to be connected；It is provided with the first solenoid valve (13) on the first idle air air inlet pipe (12), described first
It is provided on idle air escape pipe (19) second solenoid valve (42), is provided with third solenoid valve on second air inlet pipe (45)
(41), the 4th solenoid valve (43) and the 5th solenoid valve (46) are provided on the second idle air escape pipe (36)；Described first is weary
Connecting pipe is provided between wind air inlet pipe (12) and the second idle air escape pipe (36), the connecting pipe is connected to described
Between first solenoid valve (13) and the 4th solenoid valve (43), and opened by first solenoid valve (13) with the 4th solenoid valve (43)
Close its connection；It is connected between the first idle air escape pipe (19) and second air inlet pipe (45), and passes through second electricity
Magnet valve (42) opens and closes it with third solenoid valve (41) and is connected to；The first idle air escape pipe (19) and the second idle air escape pipe
(36) it is connected between, and it is opened and closed with the 5th solenoid valve (46) by the second solenoid valve (42) and is connected to.
9. a kind of coal mine methane catalytic oxidizing equipment according to claim 6, it is characterised in that: described device further includes surveying
It controls unit (40), the measurement and control unit (40) includes the first temperature sensor (7) that the gas handling system is arranged in, first pressure
Sensor (8), the first concentration sensor (9) and flowmeter (10), second be arranged on the first idle air air inlet pipe (12)
Third temperature sensor (21), the 4th temperature of the first reactor (20) is arranged in temperature sensor (15) from top to bottom
Sensor (22), the 5th temperature sensor (23) and the second pressure sensor being arranged on the first idle air escape pipe (19)
(16), the 6th temperature sensor (17), the second concentration sensor (18) are arranged in the second air inlet for entering second reactor (32)
The 7th temperature sensor on (45) is managed, the 8th temperature sensor of the second reactor (32) is set from top to bottom
(33), the 9th temperature sensor (34), the tenth temperature sensor (35), the be arranged on the second idle air escape pipe (36)
Three concentration sensors (37), third pressure sensor (38), the 11st temperature sensor (39), and be arranged in the escape pipe
(2) the 12nd temperature sensor (48) on.
10. a kind of operation method of coal mine methane catalytic oxidizing equipment, using such as the described in any item coals of claim 6 to 8
Mine idle air catalytic oxidizing equipment, which is characterized in that the described method includes:
Preheater (3) is heated；
First reactor (20) and second reactor (32) are preheated respectively；
Coal mine methane is set to enter preheater (3) preheating by gas handling system；Open the first solenoid valve (13) connection preheater (3) with
The first idle air air inlet pipe (12) between first reactor (20), the idle air after making preheating exports (11) by the first idle air and pass through the
One idle air air inlet pipe (12) enters the first reaction along the scroll casing type air inlet pipe (51) of first reactor (20) with spiral case tangential
Device (20)；
React idle air with the catalyst on the catalyst coat (28) of shell (26) inner wall in first reactor (20), it is raw
At CO2And H2O, and discharge heat；Grit in idle air is thrown to the inner wall of first reactor (20) under the action of the centrifugal force, in weight
Power acts on lower edge wall surface and falls, and is collected into storage ash bucket (31)；Open second solenoid valve (42) and third solenoid valve (41) even
The first idle air escape pipe (19) between logical first reactor (20) and second reactor (32), so that the high-temperature gas after reaction
By the gas outlet (53) of first reactor (20) by the first idle air escape pipe (19) by the air inlet of second reactor (32)
(25) enter second reactor (32)；
So that high-temperature gas and reactor shell into second reactor (32) is exchanged heat, is reacted using the heat second of carrying
Device (32), and make the idle air gas not reacted completely in first reactor (20) in second reactor (32) continuation and inner wall
Catalyst coat (28) on catalyst reaction, generate CO2And H2O, and heat is discharged, form the high-temp waste gas of fully reacting；It is high
Grit in wet body is further removed in second reactor (32)；
The 4th solenoid valve (43) and the 5th solenoid valve (46) are opened, the second idle air escape pipe (36) is made to be connected to second reactor (32)
With preheater (3), pass through the high-temp waste gas of fully reacting from second reactor (32) by the second idle air escape pipe (36) useless
Gas entrance (47) enters preheater (3), and heat recovery is carried out in preheater (3)；Under the action of air-introduced machine (1), it will drop
Exhaust gas after temperature is discharged into atmosphere by escape pipe (2)；
So that fresh coal mine methane enters preheater (3) by gas handling system, preheated under a part of heat of recycling；
Switching solenoid valve opens third solenoid valve (41) connection the second air inlet pipe (45), so that the coal mine methane after preheating passes through
Second air inlet pipe (45) by second reactor (32) air inlet (25) along scroll casing type air inlet pipe (51) with spiral case tangential into
Enter second reactor (32)；
React idle air with the catalyst on the catalyst coat (28) of shell (26) inner wall in second reactor (32), it is raw
At CO2And H2O, and discharge heat；Grit in idle air is thrown to the inner wall of second reactor (32) under the action of the centrifugal force, in weight
Power acts on lower edge wall surface and falls, and is collected into storage ash bucket (31)；High-temperature gas going out by second reactor (32) after reaction
Port (53) enters the second idle air escape pipe (36)；
The 4th solenoid valve (43) and the first solenoid valve (13) are opened, so that between second reactor (32) and first reactor (20)
The second idle air escape pipe (36), connecting pipe and the first idle air air inlet pipe (12) connection so that reaction after high-temperature gas by
The gas outlet (53) of second reactor (32) passes through the second idle air escape pipe (36), connecting pipe and the first idle air air inlet pipe (12)
First reactor (20) are entered by the air inlet (25) of first reactor (20)；
So that high-temperature gas and reactor shell into first reactor (20) is exchanged heat, is reacted using the heat first of carrying
Device (20), and make the idle air gas not reacted completely in second reactor (32) in first reactor (20) continuation and inner wall
Catalyst coat (28) on catalyst reaction, generate CO2And H2O, and heat is discharged, form the high-temp waste gas of fully reacting；It is high
Grit in wet body is further removed in first reactor (20)；
Open first between second solenoid valve (42) and the 5th solenoid valve (46) connection first reactor (20) and preheater (3)
Idle air escape pipe (19) and the second idle air escape pipe (36), so that the high-temp waste gas of fully reacting passes sequentially through the first idle air outlet
It manages (19) and the second idle air escape pipe (36) and enters preheater (3) by exhaust gas entrance (47) from first reactor (20), and
Heat recovery is carried out in preheater (3)；Under the action of air-introduced machine (1), the exhaust gas after cooling is discharged by escape pipe (2)
In atmosphere, a complete coal mine methane catalytic oxidation process is formed.
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| CN201810837037.8A CN108926996A (en) | 2015-08-10 | 2015-08-10 | A kind of cyclone type coal mine methane catalyst oxidation reactor |
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| CN101539027A (en) * | 2009-04-24 | 2009-09-23 | 北京化工大学 | Device for treating low concentration methane in ventilation air methane (VAM) of coal mine and method thereof |
| CN102205207A (en) * | 2011-04-11 | 2011-10-05 | 山东理工大学 | Coal mine methane preheating catalytic oxidation device with multiple reaction chambers |
| CN102218286A (en) * | 2011-04-11 | 2011-10-19 | 山东理工大学 | Preheating and catalytic oxidizing device of coal mine ventilation air methane |
| WO2014159440A1 (en) * | 2013-03-13 | 2014-10-02 | Basf Corporation | Cyclone particulate filtration for lean burn engines |
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| CN101539027A (en) * | 2009-04-24 | 2009-09-23 | 北京化工大学 | Device for treating low concentration methane in ventilation air methane (VAM) of coal mine and method thereof |
| CN102205207A (en) * | 2011-04-11 | 2011-10-05 | 山东理工大学 | Coal mine methane preheating catalytic oxidation device with multiple reaction chambers |
| CN102218286A (en) * | 2011-04-11 | 2011-10-19 | 山东理工大学 | Preheating and catalytic oxidizing device of coal mine ventilation air methane |
| WO2014159440A1 (en) * | 2013-03-13 | 2014-10-02 | Basf Corporation | Cyclone particulate filtration for lean burn engines |
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