CN102517109A - Fluidized bed catalytic deoxidation method and equipment for oxygen-containing coal bed gas - Google Patents
Fluidized bed catalytic deoxidation method and equipment for oxygen-containing coal bed gas Download PDFInfo
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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, and in the progress of coal mining, for guaranteeing mine safety production, a large amount of lower concentration of extraction mixes empty coal-seam gas, and its staple is methane (CH
4) and air.According to statistics, the billions of cubic meters of coal-seam gas of the annual discharging of mining of China, resource has not only been wasted in directly emptying burning of the overwhelming majority, has also increased the weight of atmospheric Greenhouse effect simultaneously, causes environmental pollution.
Methane content 30-70%, oxygen level 5-15% in the lower concentration coalbed methane containing oxygen, inflammable, explosive, the current main mode of utilizing is directly burning and generating, its economic worth fails to demonstrate fully.China's present Sweet natural gas feed rate wretched insufficiency if can it be purified, concentrate and utilize, as automobile or domestic fuel, will be effectively replenishing of natural gas source, can improve resource value and economic benefit.
The coal-seam gas purification technique mainly comprises transformation absorption, membrane sepn and low-temperature deep stripping technique etc.Transformation absorption and membrane sepn need carry out under condition of high voltage, but high pressure causes the methane limits of explosion to broaden, and will inevitably produce explosion gas in the sepn process, and operational hazards is big, are to limit coal-seam gas at present to separate the major technique factor of promoting to a higher rank and utilizing.Patent ZL85103557 discloses the method that a kind of pressure swing adsorption process separates methane in the coal-seam gas, but in the methane concentration process, also causes the increase of oxygen concn in the exhaust, has the danger of blast in the pipeline of discharging waste gas.Patent CN101531559A, CN101531560A, CN101531561A disclose the method that a kind of method that adopts low temperature fractionation is separated methane in the coal-seam gas; Adopt strict control to separate the method for curve; The limits of explosion of pilot-gas, but security is still waiting evaluation, and system risk is bigger.Therefore,, improve the security and the feasibility of technology, be necessary at first to remove blended oxygen in the coal-seam gas, and then pressurize and separate or the low-temperature liquefaction lock out operation in order to prevent gaseous detonation.
At present, the method for coal bed gas deoxidation mainly contains catalytic oxidation, coke deoxidization method etc.Patent ZL02113627.0 has announced that a kind of coalbed methane containing oxygen removes the method for oxygen through the high temperature coke pull-up, has the advantage that the methane loss is little, expense is low, but complex process, manipulation strength is big, gas aftertreatment cost is high.Patent ZL02113628.9, CN101250449A, CN101139239A, CN101613627A disclose the method that adopts catalytic deoxidation; Adopt Pt, Pd, Mn series dehydrogenation catalyst respectively; In 350-700 ℃ of scope, remove the oxygen in the coal-seam gas, the deoxidation degree can reach below 1%.From relatively seeing of the whole bag of tricks; The catalyzed oxidation method of deoxidation has utilized inherent methane and oxygen in the gas; Need not add other material; And can reclaim the used heat byproduct steam, and have that technology is simple, a deoxidation degree height, mild condition, gas aftertreatment characteristic of simple, have certain technical superiority.
The catalytic deoxidation process of coalbed methane containing oxygen is the catalytic oxidation combustion process of methane, and the exothermic heat of reaction amount is big, and how reducing and shifting out reaction heat is critical technical problems.Patent CN101139239A, CN101613627A disclose insulation fix bed coal bed gas deoxidation reactor drum; Adopt the method for the methane-rich gas of cyclic part deoxidation, reduce relative oxygen level in the coal-seam gas, thereby reduce relative thermal discharge; With the temperature of reaction of control catalyst bed in suitable scope; Prevent the local superheating overtemperature, catalyst deactivation that causes and sintering, but this also causes the energy consumption height and the production intensity of process little.
Fluidized-bed reactor is widely used in fields such as burning of coal, gasification, petroleum catalytic cracking.In the fluidized-bed reactor, solid particulate is fluidized state under the effect of gas drag force, and the gas-solid contact is effective, heat transfer, rate of mass transfer height.And fluidized-bed reactor is easy to through the built-in heat exchanger controlled temperature, is fit to very much the coal bed gas deoxidation reaction process of strong heat release.
Summary of the invention
It is good that first purpose of the present invention provides a kind of security, and energy consumption is low, and deoxidation efficient is high, and catalyst life is long, and the fluidized-bed reactor that processing power is big carries out the catalyzed oxidation method of deoxidation of coalbed methane containing oxygen.
Another object of the present invention provides the oxygen-containing coal bed gas deoxidation reaction unit that a kind of heat transfer coefficient is big, 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 made up of fluidized-bed deoxidation reactor, built-in heat exchanger, drum, cyclonic separator, standpipe, solid particulate feed back 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 the low-temperature catalytic burning reaction, generate carbonic acid gas and water, thereby oxygen content gas is reduced to below 0.5%.The low-temperature burning liberated heat is through interchanger and drum, by-product low pressure or MP steam.Coal-seam gas after the deoxidation is sent the back system handles after cyclonic separator, filter collector reclaim catalyzer.
The fluidized-bed deoxidation reactor adopts the gas-solid fluidization principle, and built-in heat exchanger is through the flow velocity and the temperature of adjustment heat exchanger heat transfer medium; Can guarantee that reactor drum is in rational service temperature; Utilize reaction heat to generate low pressure or MP steam simultaneously, reclaim heat energy, improve system's heat utilization efficiency.The gas distribution of fluidized-bed reactor has adopted multi-jet intake method, and the nozzle high cycle speed prevents tempering and detonation in the velocity of propagation of premixed flame.
The object of the invention can be realized through following technical measures:
(1) system hypothermia starts: at first drum water filling, and control drum liquid level is in safety range; Utilize the coal-seam gas baker then, preheating fluidized-bed deoxidation reactor is to 300-400 ℃, promptly more than the minimum ignition temperature of catalyzer;
(2) coalbed methane containing oxygen directly gets into the fluidized-bed deoxidation reactor from the coalbed methane containing oxygen inlet nozzle, nozzle gas speed 30-60m/s, the working pressure 0-0.4MPa (table) of controlling flow fluidized bed reactor, superficial gas velocity 0.2-2.0m/s;
(3) the particle diameter 40-1000 μ m dehydrogenation catalyst particle hopper of packing into is blowing adding fluidized-bed deoxidation reactor under the gas effect;
(4) methane in the coal-seam gas and oxygen carry out low-temperature catalytic burning reaction, gas-solid 2-10s duration of contact, temperature of reaction 350-650 ℃ in the fluidized-bed deoxidation reactor;
(5) gas-entrained part solid catalyst particle moves upward; Get into the I and II cyclonic separator from fluidized-bed deoxidation reactor top exit; The solid catalyst particle of collecting is at the feed back valve and blow under the gas control system circulation entering fluidized-bed deoxidation reactor;
(6) the deoxidation coal-seam gas after the thick dedusting of cyclonic separator send the back system to use after high-temperature filter is removed fine catalyst dust.
The volumn concentration 30-80% of methane in the aforesaid coalbed methane containing oxygen, the volumn concentration 5-15% of oxygen, the volumn concentration 20-60% of nitrogen.
The volumn concentration of oxygen is less than 0.5% in the aforesaid deoxidation coal-seam gas.
Aforesaid dehydrogenation catalyst is the spheric non-precious metal catalyst; With among Co, Fe, Cu, the Mn one or more is 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 aforesaid gas that blows can be deoxidation coal-seam gas, methane gas or nitrogen.
Aforesaid catalyst dust high-temperature filter can be sintered metal mesh strainer, sintering metal powder strainer or porcelain filter.
Aforesaid fluidized-bed deoxidation reactor is by housing, and coalbed methane containing oxygen inlet nozzle, tubular heat exchange, the outlet of deoxidation coal-seam gas, dehydrogenation catalyst particle inlet, granules of catalyst discharge gate, cooling water inlet and vapour outlet are formed, and arranges vertical tubular heat exchange in the housing; The lower end parallel connection of tubulation is connected with the cooling water inlet; The upper end parallel connection of tubulation is connected with vapour outlet, and the cooling water inlet links to each other with drum with vapour outlet, and lower part of frame is a cone; Upper and lower two row's coalbed methane containing oxygen nozzles are arranged on the cone; Cone base is the catalyzer discharge gate, and there is dehydrogenation catalyst particle inlet the side of housing, and the outlet of deoxidation coal-seam gas is arranged at the top.
The cone apex angle 60-90 of aforesaid lower housing portion taper °, be uniformly distributed with 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 °.
Aforesaid tubular heat exchange, tubulation diameter 25-89mm.
The present invention has following technical characterstic and advantage: (1) deoxygenation process adopts fluidization technology, and the gas-solid contact is effective, and heat and mass efficient is high, and processing power is big, and stable operation especially is fit 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 the catalyzer local sintering; (3) fluidized-bed reactor adopts the nozzle intake method of higher gas speed, and is 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 MP steam have improved the thermo-efficiency of system; (5) fluidized-bed reactor can be regulated 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.
Description of drawings
Fig. 1 is the structural representation of fluidized-bed deoxidation reactor.
Fig. 2 is a fluidized-bed deoxidation reactor bottom inflow structure of nozzle synoptic diagram.
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, the 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 valve; The 7th, loop seal; The 8th, the catalyst charge bucket; The 9th, high-temperature filter 1; The 10th, high-temperature filter 2; The 11st, the catalyst dust hopper; The 12nd, coalbed methane containing oxygen upper strata nozzle of air supply; The 13rd, coalbed methane containing oxygen lower floor nozzle of air supply; The 14th, vapour outlet; The 15th, the cooling water inlet; The 16th, the outlet of deoxidation coal-seam gas; The 17th, dehydrogenation catalyst particle inlet; The 18th, the granules of catalyst discharge gate; The 19th, housing.Logistics: A is a coalbed methane containing oxygen; B is a de-oxygenised water; C is a MP steam; D is the drum sewer; E is a decaying catalyst; F is a dehydrogenation catalyst; G is that catalyst charge blows gas; H is that catalyst recirculation control blows gas; I is the deoxidation coal-seam gas; J is the strainer blowback air; K is a catalyst dust.
Embodiment
Below in conjunction with accompanying drawing and embodiment embodiment of the present invention is done further to specify.
Embodiment 1
The 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 inlet 17, granules of catalyst discharge gate 18, cooling water inlet 15 and vapour outlet 14 are formed; Arrange vertical tubular heat exchange 2, tubulation diameter 25mm in the housing 19.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 links to each other with drum 3 with vapour outlet 14; The bottom of housing 1 is a cone, and two row coalbed methane containing oxygen upper strata nozzles of air supply 12 and coalbed methane containing oxygen lower floor nozzles of air supply 13 are arranged on 60 ° of cones of cone apex angle, coalbed methane containing oxygen upper strata nozzle of air supply 12 and 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 a granules of catalyst discharge gate 18, and there is dehydrogenation catalyst particle inlet 17 side of housing 1, and deoxidation coal-seam gas outlet 16 is arranged at the 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
3Coalbed 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%.460-480 ℃ of fluidized-bed deoxidation reactor service temperature, pressure are normal pressure, operating gas velocity 0.5-0.7m/s, drum pressure 1.0-1.2MPa.At first, de-oxygenised water B injects drum 3, and the control liquid level is in safety range; Then, utilize the coal-seam gas baker, 1 to 350-400 ℃ of pre-heated flow fluidized bed reactor.After fluidized-bed reactor 1 reached design temperature, coalbed methane containing oxygen A got in the housing 19 of fluidized-bed reactor 1 from nozzle of air supply 12,13, red-tape operati gas speed 0.5-0.7m/s.Dehydrogenation catalyst particle F adds hopper 8, opens catalyzer feed back valve 6, is adjusted in and blows gas G and H flow, and dehydrogenation catalyst is got in the fluidized-bed reactor 1.Granules of catalyst motion under gas entrainment and on flowing to, methane and the oxygen in the catalytic gas carries out low-temperature catalytic burning simultaneously, accomplishes deoxygenation.Heat transferring medium de-oxygenised water B gets into tubular heat exchange 2 through drum 3 through cooling water inlet 15, and high-temperature water after the heat exchange and steam return drum 3 tops through vapour outlet 14, and drum 3 produces low pressure or MP steam C, and drum sewer D discharges from the drum bottom.Control drum pressure and liquid level keep 460-480 ℃ of reactor batch temperature.The deoxidation coal-seam gas of entrained catalyst particles is discharged from deoxidation coal-seam gas outlet 16; Get into primary cyclone 4 and secondary cyclone 5 successively; Carry out gas solid separation; Isolating granules of catalyst under the control of feed back valve 6 and loop seal 7, returns fluidized-bed reactor 1 from dehydrogenation catalyst particle inlet 17 through circulating solid tube.The deoxidation coal-seam gas of carrying fine dust is removed the fine catalyst dust in the gas again through high-temperature filter 9,10.High-temperature filter 9,10 filtration pressure differences should if filtration pressure difference greater than 10KPa, carries out blocked operation, and with blowback air J blowback, clean strainer tube less than 10KPa.The volumn concentration of oxygen is 0.39% among the deoxidation coal-seam gas I of udst separation, send the back system to use.High-temperature filter 9,10 filters the catalyst fines K that collects and is collected in the hopper 11, recycles.The gas group prejudice table 1 of virgin gas of present embodiment (coalbed methane containing oxygen) and deoxidation gas.
The gas composition of table 1 embodiment 1 virgin gas and deoxidation gas
| CH 4，％ | O 2，％ | N 2，％ | CO，％ | CO2，％ | H 2，％ | |
| Virgin 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 such as instance 1 are said, 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 spheric 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
3480-500 ℃ of fluidized-bed deoxidation reactor service temperature, pressure are 0.1MPa, operating gas velocity 0.4-0.6m/s, drum pressure 1.2-1.5MPa.All the other are with instance 1.Coalbed methane containing oxygen is behind the fluidized-bed catalytic deoxidation, and the oxygen level in the deoxidation coal-seam gas is 0.35%.The gas group prejudice table 2 of virgin gas of present embodiment (coalbed methane containing oxygen) and deoxidation gas.
The gas composition of table 2 embodiment 2 virgin gass and deoxidation gas
| CH 4，％ | O 2，％ | N 2，％ | CO，％ | CO2，％ | H 2，％ | |
| Virgin 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 such as instance 1 are said.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 spheric 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
3500-520 ℃ of fluidized-bed deoxidation reactor service temperature, pressure are normal pressure, operating gas velocity 0.7-0.8m/s, drum pressure 1.0-1.2MPa.All the other are with instance 1.Coalbed methane containing oxygen is behind the fluidized-bed catalytic deoxidation, and the oxygen level in the deoxidation coal-seam gas is 0.32%.The gas group prejudice table 3 of virgin gas of present embodiment (coalbed methane containing oxygen) and deoxidation gas.
The gas composition of table 3 embodiment 3 virgin gass and deoxidation gas
| CH 4，％ | O 2，％ | N 2，％ | CO，％ | CO2，％ | H 2，％ | |
| Virgin 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 such as instance 1.Said 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 spheric 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
3520-550 ℃ of fluidized-bed deoxidation reactor service temperature, pressure are normal pressure, apparent operating gas velocity 0.7-0.8m/s, drum pressure 1.2-1.5MPa.All the other are with instance 1.Coalbed methane containing oxygen is behind the fluidized-bed catalytic deoxidation, and the oxygen level in the deoxidation coal-seam gas is 0.17%.The gas group prejudice table 4 of virgin gas of present embodiment (coalbed methane containing oxygen) and deoxidation gas.
The gas composition of table 4 embodiment 4 virgin gass and deoxidation gas
| CH 4，％ | O 2，％ | N 2，％ | CO，％ | CO2，％ | H 2，％ | |
| Virgin 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 (9)
1. the fluidized-bed catalytic deoxidation method of a coalbed methane containing oxygen is characterized in that comprising the steps:
(1) system hypothermia starts: at first drum water filling, and control drum liquid level is in safety range; Utilize the coal-seam gas baker then, preheating fluidized-bed deoxidation reactor is to 300-400 ℃, promptly more than the minimum ignition temperature of catalyzer;
(2) coalbed methane containing oxygen directly gets into the fluidized-bed deoxidation reactor from the coalbed methane containing oxygen inlet nozzle, nozzle gas speed 30-60m/s, the working pressure 0-0.4MPa of controlling flow fluidized bed reactor, superficial gas velocity 0.2-2.0m/s;
(3) the particle diameter 40-1000 μ m dehydrogenation catalyst particle hopper of packing into is blowing adding fluidized-bed deoxidation reactor under the gas effect;
(4) methane in the coal-seam gas and oxygen carry out low-temperature catalytic burning reaction, gas-solid 2-10s duration of contact, temperature of reaction 350-650 ℃ in the fluidized-bed deoxidation reactor;
(5) gas-entrained part solid catalyst particle moves upward; Get into the I and II cyclonic separator from fluidized-bed deoxidation reactor top exit; The solid catalyst particle of collecting is at the feed back valve and blow under the gas control system circulation entering fluidized-bed deoxidation reactor;
(6) the deoxidation coal-seam gas after the thick dedusting of cyclonic separator send the back system to use after high-temperature filter is removed fine catalyst dust.
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 the 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, the volumn concentration that it is characterized in that oxygen in the 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; It is characterized in that described dehydrogenation catalyst is the spheric non-precious metal catalyst, is catalytic active component with among Co, Fe, Cu, the Mn one or more, 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.
5. 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.
6. 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.
7. fluidized-bed deoxidation reactor; It is by housing (19), and coalbed methane containing oxygen inlet nozzle, tubular heat exchange (2), deoxidation coal-seam gas outlet (16), dehydrogenation catalyst particle inlet (17), granules of catalyst discharge gate (18), cooling water inlet (15) and vapour outlet (14) are formed, and arrange vertical tubular heat exchange (2) in the housing (19); 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), and cooling water inlet (15) link to each other with drum (3) with vapour outlet (14), and the bottom of housing (1) is a cone; Two row's coalbed methane containing oxygen upper strata nozzle of air supply (12) and coalbed methane containing oxygen lower floor nozzles of air supply (13) are arranged on the cone; Cone base is granules of catalyst discharge gate (18), and there is dehydrogenation catalyst particle inlet (17) side of housing (1), and deoxidation coal-seam gas outlet (16) is arranged at the top.
8. as claimed in claim 7 like a kind of fluidized-bed deoxidation reactor; It is characterized in that cone apex angle 60-90 ° of described housing (19) lower taper, coalbed methane containing oxygen upper strata nozzle of air supply (12) and coalbed methane containing oxygen lower floor nozzle of air supply (13) respectively with angle 20-60 ° of horizontal tangent to periphery.
9. as claimed in claim 7 like a kind of fluidized-bed deoxidation reactor, it is characterized in that the tubulation diameter 25-89mm of described tubular heat exchange (2).
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| 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 |
| CN108441273A (en) * | 2018-04-02 | 2018-08-24 | 东北大学 | Oxygen-containing low concentration combustible gas method of deoxidation and deoxygenation system |
| CN109764346A (en) * | 2018-12-05 | 2019-05-17 | 中国科学院山西煤炭化学研究所 | A kind of method and device of safe utilization coal bed gas |
| CN114250092A (en) * | 2022-01-12 | 2022-03-29 | 清华大学 | System and method for reducing emission of low-concentration combustible gas |
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