CN102517109B - Fluidized bed catalytic deoxidation method for oxygen-containing coal bed gas - Google Patents
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Abstract
The invention relates to a fluidized bed catalytic deoxidation method for oxygen-containing coal bed gas. The fluidized bed catalytic deoxidation method comprises the following steps that: a fluidized bed deoxidation reactor is preheated to the temperature of 300-400 DEG C; the oxygen-containing coal bed gas is fed into the fluidized bed deoxidation reactor; deoxidation catalyst granules are loaded into a feed hopper and are added into the fluidized bed deoxidation reactor under the action of air blowing and supplying; methane and oxygen in the coal bed gas are subjected to low-temperature catalytic combustion reaction in the fluidized bed deoxidation reactor; the gas moves upwards with the carrying of part of solid catalyst granules and enters a one-stage cyclone separator and a two-stage cyclone separator from the top outlet of the fluidized bed deoxidation reactor, and the collected solid catalyst granules circularly enter the fluidized bed deoxidation reactor under the control of a feed back control valve and air blowing and supplying; and the deoxidated coal bed gas which is subjected to coarse dust removal by the cyclone separators is subjected to fine catalyst dust removal by a high-temperature filter, and then, is transferred to a follow-up system for use. The fluidized bed catalytic deoxidation method for the oxygen-containing coal bed gas has the advantages of good safety, low energy consumption, high deoxidation efficiency, long service life of catalyst and large processing capacity.
Description
Technical field
The present invention relates to a kind of fluidized-bed catalytic deoxidation method and apparatus of coalbed methane containing oxygen.
Background technology
China is consumption of coal big country, in progress of coal mining, and for guaranteeing mine safety production, the mixed empty coal-seam gas of lower concentration that extraction is a large amount of, its main component is methane (CH
4) and air.According to statistics, the billions of cubic meters of coal-seam gas that China mines every year and discharges, directly emptying burning of the overwhelming majority, has not only wasted resource, and the Greenhouse effect that the while has also been increased the weight of atmosphere, cause environmental pollution.
Methane content 30-70%, oxygen level 5-15% in lower concentration coalbed methane containing oxygen, inflammable, explosive, the current main mode of utilizing is directly burning and generating, its economic worth fails to fully demonstrate.China's current Sweet natural gas feed rate wretched insufficiency, if can be purified, concentrate and utilize, as automobile or domestic fuel, will be effectively supplementing of natural gas source, can improve resource value and economic benefit.
Coal-seam gas purification technique mainly comprises pressure-variable adsorption, membrane sepn and low-temperature deep isolation technique etc.Pressure-variable adsorption and membrane sepn need to carry out under condition of high voltage, but high pressure causes methane limits of explosion to broaden, and will inevitably produce explosion gas in sepn process, and operational hazards is large, are to limit at present the major technique factor that coal-seam gas separation is promoted to a higher rank and utilized.Patent ZL85103557 discloses the method for methane in the separated coal-seam gas of a kind of pressure swing adsorption process, but in methane concentration process, also causes the increase of oxygen concn in exhaust, has the danger of blast in the pipeline of discharging waste gas.Patent CN101531559A, CN101531560A, CN101531561A discloses the method for methane in the separated coal-seam gas of a kind of method that adopts low temperature fractionation, adopt the strict method of controlling detach Spline, control the limits of explosion of gas, but security need evaluation, system risk is larger.Therefore, in order to prevent gaseous detonation, improve security and the feasibility of technique, be necessary first to remove the oxygen mixing in coal-seam gas, and then carry out separation or low-temperature liquefaction lock out operation.
At present, the method for coal bed gas deoxidation mainly contains catalytic oxidation, coke deoxidization method etc.Patent ZL02113627.0 announced a kind of coalbed methane containing oxygen by high temperature coke pull-up except the method for oxygen, have advantages of that methane loss is little, expense is low, but complex process, manipulation strength is large, gas aftertreatment cost is high.Patent ZL02113628.9, CN101250449A, CN101139239A, CN101613627A disclose the method that adopts catalytic deoxidation, adopt respectively Pt, Pd, Mn series dehydrogenation catalyst, within the scope of 350-700 ℃, remove the oxygen in coal-seam gas, deoxidation degree can reach below 1%.From the whole bag of tricks relatively, catalyzed oxidation method of deoxidation has utilized methane and oxygen intrinsic in gas, do not need to add other material, and can reclaim used heat byproduct steam, have that technique is simple, deoxidation degree is high, mild condition, the simple feature of gas aftertreatment, there is certain technical superiority.
The catalytic deoxidation process of coalbed methane containing oxygen is the catalytic oxidation combustion process of methane, and exothermic heat of reaction amount is large, and how reducing and shifting out reaction heat is crucial technical problem.Patent CN101139239A, CN101613627A disclose insulation fix bed coal bed gas deoxidation reactor, adopt the method for the methane-rich gas of cyclic part deoxidation, reduce relative oxygen level in coal-seam gas, thereby reduce relative thermal discharge, with the temperature of reaction of controlling beds in suitable scope, prevent local superheating overtemperature, the catalyst deactivation causing and sintering, but this also causes energy consumption height and the production intensity of process little.
Fluidized-bed reactor is widely used in the fields such as burning of coal, gasification, petroleum catalytic cracking.In fluidized-bed reactor, solid particulate, under the effect of gas drag force, is fluidized state, and gas-solid contact is effective, conducts heat, rate of mass transfer is high.And fluidized-bed reactor is easy to control temperature by built-in heat exchanger, be applicable to very much the coal bed gas deoxidation reaction process of strong heat release.
Summary of the invention
It is good that first object of the present invention is to provide a kind of security, and energy consumption is low, and deoxidation efficiency is high, and catalyst life is long, and the fluidized-bed reactor that processing power is large carries out the catalyzed oxidation method of deoxidation of coalbed methane containing oxygen.
Another object of the present invention is to provide the oxygen-containing coal bed gas deoxidation reaction unit that a kind of heat transfer coefficient is large, heat exchange efficiency is high, security is good, simple in structure.
The fluidized-bed method of deoxidation of a kind of coalbed methane containing oxygen of the present invention is comprised of fluidized-bed deoxidation reactor, built-in heat exchanger, drum, cyclonic separator, standpipe, solid particulate feed back control valve, catalyst dust high-temperature filter.In fluidized-bed reactor, utilize spherical base metal dehydrogenation catalyst, methane and oxygen in red-tape operati pressure 0-0.4MPa (table), temperature 350-650 ℃, coalbed methane containing oxygen carry out low-temperature catalytic burning reaction, generate carbonic acid gas and water, thereby oxygen content gas is reduced to below 0.5%.Low-temperature burning liberated heat is through interchanger and drum, by-product low pressure or middle pressure steam.Coal-seam gas after deoxidation reclaims after catalyzer through cyclonic separator, filter collector, send rear system to process.
Fluidized-bed deoxidation reactor adopts gas-solid fluidization principle, and built-in heat exchanger, by adjusting flow velocity and the temperature of heat exchanger heat transfer medium, can guarantee that reactor is in rational service temperature, utilize reaction heat to generate low pressure or middle pressure steam simultaneously, reclaim heat energy, improve system heat utilization efficiency.The gas distribution of fluidized-bed reactor, has adopted multi-jet intake method, and nozzle high cycle speed, in the velocity of propagation of premixed flame, prevents tempering and detonation.
Object of the present invention can realize by following technical measures:
(1) system hypothermia starts: first drum water filling, control liquid level of steam drum in safety range; Then utilize coal-seam gas baker, preheating fluidized-bed deoxidation reactor is to 300-400 ℃, more than the minimum ignition temperature of catalyzer;
(2) coalbed methane containing oxygen directly enters fluidized-bed deoxidation reactor from coalbed methane containing oxygen inlet nozzle, nozzle gas speed 30-60m/s, the working pressure 0-0.4MPa (table) of control fluidized-bed reactor, superficial gas velocity 0.2-2.0m/s;
(3) particle diameter 40-1000 μ m dehydrogenation catalyst particle packs hopper into, adds fluidized-bed deoxidation reactor blowing under gas effect;
(4) methane in coal-seam gas and oxygen carry out low-temperature catalytic burning reaction, gas-solid contact time 2-10s, temperature of reaction 350-650 ℃ in fluidized-bed deoxidation reactor;
(5) gas carries part solid catalyst particle and moves upward, from fluidized-bed deoxidation reactor top exit, enter I and II cyclonic separator, the solid catalyst particle of collecting is at feed back control valve and blow under gas control system, and circulation enters fluidized-bed deoxidation reactor;
(6) the deoxidation coal-seam gas after the thick dedusting of cyclonic separator, after high-temperature filter is removed fine catalyst dust, send rear system to use.
The volumn concentration 30-80% of methane in coalbed methane containing oxygen as above, the volumn concentration 5-15% of oxygen, the volumn concentration 20-60% of nitrogen.
In deoxidation coal-seam gas as above, the volumn concentration of oxygen is less than 0.5%.
Dehydrogenation catalyst as above is spherical non-precious metal catalyst, one or more of take in Co, Fe, Cu, Mn are catalytic active component, active component content 5-30%, alumina content 70-90%, other metal promoter content 2-10%, catalyst particle size 40-1000 μ m, pore volume 0.45-0.75cm
3/ g, bulk density 0.6-1.0g/ml.
The gas that blows as above can be deoxidation coal-seam gas, methane gas or nitrogen.
Catalyst dust high-temperature filter as above can be sintered metal mesh strainer, sintering metal powder strainer or porcelain filter.
Fluidized-bed deoxidation reactor as above is by housing, coalbed methane containing oxygen inlet nozzle, tubular heat exchange, the outlet of deoxidation coal-seam gas, dehydrogenation catalyst particle entrance, granules of catalyst discharge gate, cooling water inlet and vapour outlet form, in housing, arrange vertical tubular heat exchange, the lower end parallel connection of tubulation is connected with cooling water inlet, the upper end parallel connection of tubulation is connected with vapour outlet, cooling water inlet is connected with drum with vapour outlet, the bottom of housing is cone, on having in cone, lower two row's coalbed methane containing oxygen nozzles, cone base is catalyzer discharge gate, there is dehydrogenation catalyst particle entrance the side of housing, the outlet of deoxidation coal-seam gas is arranged at top.
The cone apex angle 60-90 ° of lower housing portion taper as above, uniform two row's nozzles of air supply on the conical surface, the angle 20-60 ° of nozzle of air supply and horizontal tangent to periphery.
Tubular heat exchange as above, tubulation diameter 25-89mm.
The present invention has following technical characterstic and advantage: (1) deoxygenation process adopts fluidization technology, and gas-solid contact is effective, and heat and mass efficiency is high, and processing power is large, and stable operation is especially applicable to the higher gas treating process of oxygen level; (2) the built-in interchanger of fluidized-bed can shift out reaction heat fast, keeps bed temperature even, improves reactive behavior and selectivity, prevents catalyzer local sintering; (3) fluidized-bed reactor adopts the nozzle intake method of higher gas speed, simple in structure, and can prevent the tempering or the detonation that cause because of gas composition or fluctuation of pressure drop, and security is good; (4) deoxygenation process by-product low pressure or middle pressure steam, improved the thermo-efficiency of system; (5) fluidized-bed reactor can regulate the flow velocity of bed gas speed and heat transferring medium water according to actual treatment tolerance, and anti-fluctuation of load ability is strong; (6) device structure is simple, and flexible operation is easy to industry and amplifies.
Accompanying drawing explanation
Fig. 1 is the structural representation of fluidized-bed deoxidation reactor.
Fig. 2 is the structural representation of fluidized-bed deoxidation reactor bottom inflow nozzle.
Fig. 3 is the process flow diagram of the fluidized-bed catalytic deoxidation method of a kind of coalbed methane containing oxygen of the present invention.
As shown in the figure, the 1st, fluidized-bed deoxidation reactor; The 2nd, tubular heat exchange; The 3rd, drum; The 4th, primary cyclone; The 5th, secondary cyclone; The 6th, catalyzer feed back control valve; The 7th, loop seal; The 8th, catalyst charge bucket; The 9th, high-temperature filter 1; The 10th, high-temperature filter 2; The 11st, catalyst dust hopper; The 12nd, coalbed methane containing oxygen upper strata nozzle of air supply; 13Shi coalbed methane containing oxygen lower floor nozzle of air supply; The 14th, vapour outlet; The 15th, cooling water inlet; The 16th, the outlet of deoxidation coal-seam gas; The 17th, dehydrogenation catalyst particle entrance; The 18th, granules of catalyst discharge gate; The 19th, housing.Logistics: A is coalbed methane containing oxygen; B is de-oxygenised water; C is middle pressure steam; D is drum sewer; E is decaying catalyst; F is dehydrogenation catalyst; G is that catalyst charge blows gas; H is that catalyst recirculation control blows gas; I is deoxidation coal-seam gas; J is strainer blowback air; K is catalyst dust.
Embodiment
Below in conjunction with drawings and Examples, embodiments of the present invention are described in further detail.
Embodiment 1
Fluidized-bed deoxidation reactor is by housing 19, coalbed methane containing oxygen inlet nozzle, tubular heat exchange 2, deoxidation coal-seam gas outlet 16, dehydrogenation catalyst particle entrance 17, granules of catalyst discharge gate 18, cooling water inlet 15 and vapour outlet 14 form, the tubular heat exchange 2 that the interior layout of housing 19 is vertical, tubulation diameter 25mm.The lower end parallel connection of tubulation is connected with cooling water inlet 15, the upper end parallel connection of tubulation is connected with vapour outlet 14, cooling water inlet 15 is connected with drum 3 with vapour outlet 14, the bottom of housing 1 is cone, in 60 ° of cones of cone apex angle, have two row's coalbed methane containing oxygen upper strata nozzle of air supply 12He coalbed methane containing oxygen lower floor nozzles of air supply 13, coalbed methane containing oxygen upper strata nozzle of air supply 12He coalbed methane containing oxygen lower floor nozzle of air supply 13 respectively with 25 ° of the angles of horizontal tangent to periphery.Cone base is granules of catalyst discharge gate 18, and there is dehydrogenation catalyst particle entrance 17 side of housing 1, and deoxidation coal-seam gas outlet 16 is arranged at top.
The high 8000mm of fluidized-bed deoxidation reactor, internal diameter 300mm.Dehydrogenation catalyst is spherical cobalt-base catalyst (cobalt oxide content 10%, alumina content 85%, other metal promoter content 5%), particle diameter 40-200 μ m, bulk density 0.62g/cm
3.Coalbed methane containing oxygen consist of (percentage by volume): CH
4content 52.40%, O
2content 9.93%, N
2content 37.36%, other gas content 0.31%.Fluidized-bed deoxidation reactor service temperature 460-480 ℃, pressure is normal pressure, operating gas velocity 0.5-0.7m/s, drum pressure 1.0-1.2MPa.First, de-oxygenised water B injects drum 3, controls liquid level in safety range; Then, utilize coal-seam gas baker, pre-heated flow fluidized bed reactor 1 is to 350-400 ℃.Fluidized-bed reactor 1 reaches after design temperature, and coalbed methane containing oxygen A enters from nozzle of air supply 12,13 in the housing 19 of fluidized-bed reactor 1, red-tape operati gas speed 0.5-0.7m/s.Dehydrogenation catalyst particle F adds hopper 8, opens catalyzer feed back control valve 6, is adjusted in and blows gas G and H flow, and dehydrogenation catalyst is entered in fluidized-bed reactor 1.Granules of catalyst under gas entrainment and stream move upward, simultaneously methane and the oxygen in catalytic gas carries out low-temperature catalytic burning, completes deoxygenation.Heat transferring medium de-oxygenised water B enters tubular heat exchange 2 through drum 3 by cooling water inlet 15, and the high temperature water and steam after heat exchange, through vapour outlet 14, returns to drum 3 tops, and drum 3 produces low pressure or middle pressure steam C, and drum sewer D discharges from drum bottom.Control drum pressure and liquid level, keep reactor batch temperature 460-480 ℃.The deoxidation coal-seam gas of entrained catalyst particles is discharged from deoxidation coal-seam gas outlet 16, enter successively primary cyclone 4 and secondary cyclone 5, carry out gas solid separation, separated granules of catalyst under the control of feed back control valve 6 and loop seal 7, returns to fluidized-bed reactor 1 from dehydrogenation catalyst particle entrance 17 through circulating solid tube.Carry the deoxidation coal-seam gas of fine dust again through high- temperature filter 9,10, remove the fine catalyst dust in gas.High- temperature filter 9,10 filtration pressure differences should be less than 10KPa, if filtration pressure difference is greater than 10KPa, carry out blocked operation, and with blowback air J blowback, clean strainer tube.In the deoxidation coal-seam gas I of udst separation, the volumn concentration of oxygen is 0.39%, send rear system to use.High- temperature filter 9,10 filters the catalyst fines K collecting and is collected in hopper 11, recycles.The gas composition of the unstripped gas of the present embodiment (coalbed methane containing oxygen) and deoxidation gas is in Table 1.
The gas composition of table 1 embodiment 1 unstripped gas and deoxidation gas
| CH 4，％ | O 2，％ | N 2，％ | CO，％ | CO2，％ | H 2，％ | |
| Unstripped gas | 52.40 | 9.93 | 37.36 | ----- | 0.11 | 0.20 |
| Deoxidation gas | 52.81 | 0.39 | 41.51 | 0.03 | 5.24 | 0.02 |
The structure of fluidized-bed deoxidation reactor as described in Example 1, the tubulation diameter 38mm of tubular heat exchange, 90 ° of fluidized-bed reactor bottom cone apex angles.
Coalbed methane containing oxygen consist of (percentage by volume): CH
4content 52.40%, O
2content 9.93%, N
2content 37.36%, other gas content 0.23%.Dehydrogenation catalyst is spherical cobalt-base catalyst (cobalt oxide content 30%, alumina content 67%, other metal promoter content 3%), and particle diameter is 40-200 μ m, bulk density 0.65g/cm
3.Fluidized-bed deoxidation reactor service temperature 480-500 ℃, pressure is 0.1MPa, operating gas velocity 0.4-0.6m/s, drum pressure 1.2-1.5MPa.All the other are with example 1.Coalbed methane containing oxygen is after fluidized-bed catalytic deoxidation, and the oxygen level in deoxidation coal-seam gas is 0.35%.The gas composition of the unstripped gas of the present embodiment (coalbed methane containing oxygen) and deoxidation gas is in Table 2.
The gas composition of table 2 embodiment 2 unstripped gass and deoxidation gas
| CH 4，％ | O 2，％ | N 2，％ | CO，％ | CO2，％ | H 2，％ | |
| Unstripped gas | 52.40 | 9.93 | 37.36 | ----- | 0.11 | 0.20 |
| Deoxidation gas | 52.82 | 0.35 | 41.58 | 0.02 | 5.21 | 0.02 |
Embodiment 3
The structure of fluidized-bed deoxidation reactor as described in Example 1.Coalbed methane containing oxygen consist of (percentage by volume): CH
4content 68.27%, O
2content 6.58%, N
2content 24.80%, other gas content 0.35%.Dehydrogenation catalyst is spherical copper-based catalysts (cupric oxide content 8%, alumina content 87%, other metal promoter content 5%), and particle diameter is 60-240 μ m, bulk density 0.68g/cm
3.Fluidized-bed deoxidation reactor service temperature 500-520 ℃, pressure is normal pressure, operating gas velocity 0.7-0.8m/s, drum pressure 1.0-1.2MPa.All the other are with example 1.Coalbed methane containing oxygen is after fluidized-bed catalytic deoxidation, and the oxygen level in deoxidation coal-seam gas is 0.32%.The gas composition of the unstripped gas of the present embodiment (coalbed methane containing oxygen) and deoxidation gas is in Table 3.
The gas composition of table 3 embodiment 3 unstripped gass and deoxidation gas
| CH 4，％ | O 2，％ | N 2，％ | CO，％ | CO2，％ | H 2，％ | |
| Unstripped gas | 68.27 | 6.58 | 24.80 | ----- | 0.14 | 0.21 |
| Deoxidation gas | 69.55 | 0.32 | 26.52 | 0.10 | 3.49 | 0.02 |
Embodiment 4
The structure of fluidized-bed deoxidation reactor is as example 1.Described coalbed methane containing oxygen consist of (percentage by volume): CH
4content 31.57%, O
2content 14.32%, N
2content 53.88%, other gas content 0.23%.Dehydrogenation catalyst is spherical copper-based catalysts (cupric oxide content 15%, alumina content 80%, other metal promoter content 5%), and particle diameter is 60-240 μ m, bulk density 0.68g/cm
3.Fluidized-bed deoxidation reactor service temperature 520-550 ℃, pressure is normal pressure, apparent operating gas velocity 0.7-0.8m/s, drum pressure 1.2-1.5MPa.All the other are with example 1.Coalbed methane containing oxygen is after fluidized-bed catalytic deoxidation, and the oxygen level in deoxidation coal-seam gas is 0.17%.The gas composition of the unstripped gas of the present embodiment (coalbed methane containing oxygen) and deoxidation gas is in Table 4.
The gas composition of table 4 embodiment 4 unstripped gass and deoxidation gas
| CH 4，％ | O 2，％ | N 2，％ | CO，％ | CO2，％ | H 2，％ | |
| Unstripped gas | 31.57 | 14.32 | 53.88 | ----- | 0.10 | 0.13 |
| Deoxidation gas | 28.55 | 0.17 | 62.75 | 0.11 | 8.40 | 0.02 |
Claims (5)
1. a fluidized-bed catalytic deoxidation method for coalbed methane containing oxygen, is characterized in that comprising the steps:
System hypothermia starts: first drum water filling, control liquid level of steam drum in safety range; Then utilize coal-seam gas baker, preheating fluidized-bed deoxidation reactor is to 300-400 ℃, more than the minimum ignition temperature of catalyzer;
Coalbed methane containing oxygen directly enters fluidized-bed deoxidation reactor from coalbed methane containing oxygen inlet nozzle, nozzle gas speed 30-60m/s, the working pressure 0-0.4MPa of control fluidized-bed reactor, superficial gas velocity 0.2-2.0m/s;
Particle diameter 40-1000 μ m dehydrogenation catalyst particle packs hopper into, adds fluidized-bed deoxidation reactor blowing under gas effect;
Methane in coal-seam gas and oxygen carry out low-temperature catalytic burning reaction, gas-solid contact time 2-10s, temperature of reaction 350-650 ℃ in fluidized-bed deoxidation reactor;
Gas carries part solid catalyst particle and moves upward, and from fluidized-bed deoxidation reactor top exit, enters I and II cyclonic separator, and the solid catalyst particle of collection is at feed back control valve and blowing under gas control system, and circulation enters fluidized-bed deoxidation reactor;
Deoxidation coal-seam gas after the thick dedusting of cyclonic separator, after high-temperature filter is removed fine catalyst dust, send rear system to use;
Described dehydrogenation catalyst is spherical non-precious metal catalyst, and one or more of take in Fe, Cu, Mn are catalytic active component, active component content 5-30%, alumina content 70-90%, other metal promoter content 2-10%, catalyst particle size 40-1000 μ m, pore volume 0.45-0.75cm
3/ g, bulk density 0.6-1.0g/ml.
2. the fluidized-bed catalytic deoxidation method of a kind of coalbed methane containing oxygen as claimed in claim 1, is characterized in that the volumn concentration 30-80% of methane in described coalbed methane containing oxygen, the volumn concentration 5-15% of oxygen, the volumn concentration 20-60% of nitrogen.
3. the fluidized-bed catalytic deoxidation method of a kind of coalbed methane containing oxygen as claimed in claim 1, is characterized in that the volumn concentration of oxygen in described deoxidation coal-seam gas is less than 0.5%.
4. the fluidized-bed catalytic deoxidation method of a kind of coalbed methane containing oxygen as claimed in claim 1, is characterized in that the described gas that blows is deoxidation coal-seam gas, methane gas or nitrogen.
5. the fluidized-bed catalytic deoxidation method of a kind of coalbed methane containing oxygen as claimed in claim 1, is characterized in that described high-temperature filter is sintered metal mesh strainer, sintering metal powder strainer or porcelain filter.
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| CN104774652B (en) * | 2015-03-31 | 2018-07-20 | 成都易态科技有限公司 | Coal reburner flue gas cleaning system |
| CN106390742A (en) * | 2016-09-23 | 2017-02-15 | 河北工业大学 | Flue gas denitration reaction catalyzing device |
| CN106475019A (en) * | 2016-11-16 | 2017-03-08 | 中国科学院山西煤炭化学研究所 | A kind of fluidized-bed reactor for being catalyzed combustion deoxidizing for colliery high concentration gas extraction gas |
| CN108441273B (en) * | 2018-04-02 | 2019-12-24 | 东北大学 | Oxygen-containing low-concentration combustible gas deoxidation method and deoxidation system |
| CN109764346B (en) * | 2018-12-05 | 2020-06-30 | 中国科学院山西煤炭化学研究所 | Method and device for safely utilizing coal bed gas |
| CN114250092B (en) * | 2022-01-12 | 2023-04-25 | 清华大学 | System and method for reducing emission of low-concentration combustible gas |
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