CN101508924B - Catalysis deoxidization process for coal bed gas of coal mine zone - Google Patents
Catalysis deoxidization process for coal bed gas of coal mine zone Download PDFInfo
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Abstract
The invention discloses a coal bed gas catalytic deoxidation technique in coal field, which adopts a multistage reactor for multilevel catalytic deoxidation reaction to control the temperature of gas at the inlet of every stage of reactor and the content of O2 in the gas at the inlet, so as to ensure the temperature of gas at the outlet of every stage of reactor to be less than or equal to 660 DEG C after the catalytic deoxidation reaction. Compared with an individual reactor, the deoxidation technique of the invention can greatly reduce the quantity of the gas that is taken as return gas and used for diluting O2 in the coal bed gas of the raw materials, thus reducing the energy consumption; meanwhile, the temperature of the gas at the outlet of the deoxidation reactor can be effectively controlled to be lower than 660 DEG C, the cracking of methane can be reduced, and the loss of the methane can be obviously lowered.
Description
Technical field
The present invention relates to coal field gas utilization technical field, especially a kind of catalytic deoxidation process of coal field coal-seam gas.
Background technology
China's coal bed gas resource is abundant, and prognostic resources is about 31,000,000,000,000 m
3, be world's coal-seam gas the 3rd reserves state, in coal mining, will discharge a large amount of coal-seam gas every year in atmosphere, polluted atmospheric environment.
The coal field coal-seam gas is the gas that is rich in methane, is a kind of clean fuel.Outstanding along with the nervous trend of world energy sources and environmental problem also paid attention to the utilization of coal-seam gas further.At present, China's coal-seam gas is that the down-hole is extracted in a large number, the principal security safety in production.The coal-seam gas that its discharging obtains (CMM) methane content is not high, 30%-60% (percent by volume) only, and fluctuate with the variation of mining environment.
For the coal-seam gas of a large amount of medium methane contents (30%-60%), can do domestic fuel, PW usefulness gas and generating usually.Because civilian limited, generating efficiency is lower, so the coal-seam gas of extracting out mostly enters atmosphere, both wasted resource, polluted environment again.
In order to enlarge other purposes of this type of coal-seam gas, need to improve methane concentration, no matter be pressure swing adsorption process, or low ternperature separation process concentrate, because the concentration of oxygen is high in the coal-seam gas, before concentrating, must remove oxygen, to get rid of explosion hazard.And the collocation method of deoxidization technique flow process is one of key of deoxidization technique.
Adopting catalytic deoxidation is a kind of effective method of deoxidation.Its principal reaction formula is:
CH
4+2O
2＝CO
2+2H
2O
This reaction is a strong exothermal reaction, and temperature rise is big.According to calculating the coal-seam gas contain below 50% methane, whenever remove 1% oxygen temperature rise more than 85 ℃, to look oxygen level in the coal-seam gas and decide, oxygen level heals high temperature rise more greatly.As containing the coal-seam gas single pass reaction of 10% oxygen, temperature will make a large amount of cracking of methane up to more than 1000 ℃, cause the methane loss.
Summary of the invention
The purpose of this invention is to provide a kind of catalysis deoxidization process for coal bed gas of coal mine zone, utilize this technology that the deoxidation reactor Outlet Gas Temperature is controlled at below 660 ℃, power consumption of circulation and compression is reduced greatly.
In order to realize the foregoing invention purpose, the technical scheme that the present invention adopts is following:
A kind of catalysis deoxidization process for coal bed gas of coal mine zone adopts staged reactor (being deoxidation reactor) to carry out multistage catalytic deoxidation reaction, controls O in gasinlet temperature and the inlet gas of each stage reactor
2Content makes the Outlet Gas Temperature of each stage reactor of catalytic deoxidation reaction back equal≤660 ℃.
Preferred scheme, O in the inlet gas of each stage reactor of may command
2Content≤3.5%; Available control method is following:
(1) inlet gas of first step reactor drum control:
Adopt part deoxidation and cooled gas (product gas) to join in the coal-seam gas of feed coal mining area, be diluted to wherein O as returning gas
2Content≤3.5%;
(2) inlet gas of other each stage reactor (except the first step reactor drum) control:
Feed coal mining area coal-seam gas is joined in previous stage catalytic deoxidation reaction and the cooled gas (promptly the A reactor gas that exports out) in the past, and the amount that adds feed coal mining area coal-seam gas is so that O wherein after the adding
2Content≤3.5% is advisable.
Further preferred; Can with the reacted gas of previous stage catalytic deoxidation (because the catalytic deoxidation reaction takes place in reactor drum; The gas temperature rise of reaction back is big) with water cooling and produce steam (vapor pressure can reach more than the 3.4MPa); Rely on the gas temperature behind the controlled chilling to make its and the feed coal mining area mixed temperature of coal-seam gas reach 330 ℃ ± 10 ℃ of dehydrogenation catalyst starting temperatures, get into again and carry out catalytic deoxidation in the reactor drum of corresponding stage and react.
The staged reactor that adopts in the above-mentioned catalytic deoxidation reaction process can be preferably the 2-4 level.
In each stage reactor, being used for the catalytic deoxidation catalyst for reaction and can selecting various coal bed gas deoxidation catalysts commonly used for use, is dehydrogenation catalyst etc. like various manganese.
Compared with prior art, the invention has the beneficial effects as follows: still do not have special-purpose coal bed gas deoxidation full scale plant at present,, compare, can make as returning gas to be used for diluting raw material coal-seam gas O with adopting single reactor drum through deoxidization technique of the present invention
2The product tolerance of content reduces greatly, thereby has reduced energy consumption; The gas temperature that can effectively control simultaneously the deoxidation reactor outlet is below 660 ℃ in temperature, can reduce methane cracking, reduces the methane loss amount.
Description of drawings
Fig. 1 is 2 grades of catalytic deoxidation reaction process schematic flow sheets of the embodiment of the invention 1 coal field coal-seam gas;
Fig. 2 is 3 grades of catalytic deoxidation reaction process schematic flow sheets of the embodiment of the invention 2 coal field coal-seam gas;
Fig. 3 is 4 grades of catalytic deoxidation reaction process schematic flow sheets of the embodiment of the invention 3 coal field coal-seam gas.
Among Fig. 1-3, R1-R4 is the first step a to fourth stage reactor drum, and B1-B4 is a steam boiler, and E1 and E2 are interchanger, and P is a compressor, and 0 is the raw material coal-seam gas, and 1-21 is the pipeline of different sections.
Embodiment
Below in conjunction with embodiment the present invention is made further detailed description.
But should this be interpreted as that the scope of the above-mentioned theme of the present invention only limits to following embodiment.
Comparative Examples 1
This example is the Comparative Examples of embodiment 1-3:
The raw material coal-seam gas is formed (vol% is butt, down together): CH
450, O
210.5, N
239.5.Tolerance is 30000Nm
3/ h, deoxygenation adopt a reactor drum, and advancing the reactor drum oxygen concn is 3.5%, and then recycle ratio is 2 (recycle ratio is meant the ratio of the product gas that is used for diluting oxygen in the coal-seam gas and the coal-seam gas total amount of need deoxidation), and promptly diluting tolerance is 60000Nm
3/ h, the pressure that advances deoxidation reactor is 0.6MPa, 330 ℃ of temperature.Go out 630 ℃ of temperature of reactor, O
2＜0.1%, pressure is 0.45MPa behind heat exchange refrigerated separation water.
Carrier gas is compressed to 0.6MPa from pressure 0.45MPa, compression power consumption 914kWh.
The catalytic deoxidation reaction process of present embodiment coal field coal-seam gas is as shown in Figure 1, adopts 2 stage reactors to carry out 2 grades of catalytic deoxidation reactions:
Coal field coal-seam gas (raw material coal-seam gas) consists of (vol%): CH
450, O
210.5, N
239.5.Tolerance is 30000Nm
3/ h, 120 ℃ of temperature, pressure 0.6MPa.
The raw material coal-seam gas is divided into two portions and (is respectively 12000Nm
3/ h and 18000Nm
3/ h) get into the first step and second stage reactor drum respectively:
40% of raw material coal-seam gas total amount is 12000Nm
3/ h (raw material coal-seam gas 0) gets into pipeline 1, with the 24000Nm from pipeline 13
3/ h (422 ℃ of temperature) returns gas to be mixed, and mixes O in the gas of back
2Content is 3.5%, and 330 ℃ of temperature get among the first step reactor drum R1 through pipeline 3, under catalyst action, carry out the reaction of first step catalytic deoxidation; Reacted gas gets into pipeline 4 from first step reactor drum R1 outlet, and the exit gas temperature is 630 ℃, wherein O
2＜0.1%; With water cooling and produce steam, the gas temperature behind the controlled chilling is 422 ℃ to this gas in steam boiler B1, gets into pipeline 5;
Raw material coal-seam gas total amount 60% be 18000Nm in addition
3/ h joins in the pipeline 5 through pipeline 2, mixes with reaction of first step catalytic deoxidation and cooled gas, and after the mixing, O
2Be 3.5%, 330 ℃ of temperature in pipeline 6 entering second stage reactor drum R2, under catalyst action, are carried out second stage catalytic deoxidation reaction; Reactor drum R2 outlet gets into pipeline 7,631 ℃ of exit gas temperatures, wherein O to reacted gas from the second stage
2＜0.1%;
Catalytic deoxidation reacted gas in the second stage gets into interchanger E1, gets into steam boiler B2, gets into interchanger E2 cooling through pipeline 9 then through pipeline 8 again through pipeline 7; Divide again and dried uply (do not mark water separator among the figure; Down together); Gaseous tension 0.45Mpa after branch is dried up gets into pipeline 10, obtains 50850Nm
3/ h deoxidation gas (being product gas), wherein 26850Nm
3/ h is as the output of product gas, 24000Nm in addition
3/ h gets into pipeline 11 as returning gas; P is pressurized to 0.6MPa through compressor; Get into interchanger E1 heating through pipeline 12 again; Get into pipeline 1 through pipeline 13 then and mix, get into the first deoxidation reactor R1 (can move continuously according to above-mentioned technical process, realize continuing to produce) through pipeline 3 again with raw material coal-seam gas 0.
In the present embodiment, as the 24000Nm that returns gas
3/ h deoxidation gas is compressed to 0.6MPa by pressure 0.45MPa, and compression power consumption is 366kWh only.
The catalytic deoxidation reaction process of present embodiment coal field coal-seam gas is as shown in Figure 2, adopts 3 stage reactors to carry out 3 grades of catalytic deoxidation reactions:
Coal field coal-seam gas (raw material coal-seam gas) consists of (vol%): CH
450, O
210.5, N
239.5.Tolerance is 30000Nm
3/ h, 120 ℃ of temperature, pressure 0.6MPa.
The raw material coal-seam gas is divided into three parts and (is respectively 7500Nm
3/ h, 10500Nm
3/ h and 12000Nm
3/ h) get into the first step, the second stage and third stage reactor drum respectively:
The 7500Nm of first part
3/ h raw material coal-seam gas 0 gets into pipeline 1, with the 15000Nm from pipeline 17
3/ h (422 ℃ of temperature) returns gas to be mixed, and mixes O in the gas of back
2Content is 3.5%, and 330 ℃ of temperature get among the first step reactor drum R1 through pipeline 4, under catalyst action, carry out the reaction of first step catalytic deoxidation; Reacted gas gets into pipeline 5 from first step reactor drum R1 outlet, and the exit gas temperature is 629 ℃, wherein O
2＜0.1%; With water cooling and produce steam, the gas temperature behind the controlled chilling is 416 ℃ to this gas in steam boiler B1, gets into pipeline 6;
The 10500Nm of second section
3/ h raw material coal-seam gas 0 joins in the pipeline 6 through pipeline 2, mixes with reaction of first step catalytic deoxidation and cooled gas, mixes back O
2Be 3.35%, 330 ℃ of temperature in pipeline 7 entering second stage reactor drum R2, under catalyst action, are carried out second stage catalytic deoxidation reaction; Reactor drum R2 outlet gets into pipeline 8,619 ℃ of exit gas temperatures, wherein O to reacted gas from the second stage
2＜0.1%; With water cooling and produce steam, the gas temperature behind the controlled chilling is 398 ℃ to this gas in steam boiler B2, gets into pipeline 9;
The 12000Nm of third part
3/ h raw material coal-seam gas 0 joins in the pipeline 9 through pipeline 3, mixes with reaction of second stage catalytic deoxidation and cooled gas, and after the mixing, O
2Be 2.8%, 330 ℃ of temperature get among the third stage reactor drum R3 through pipeline 10, under catalyst action, carry out the reaction of third stage catalytic deoxidation; Reacted gas gets into pipeline 11,573 ℃ of exit gas temperatures, wherein O from third stage reactor drum R3 outlet
2＜0.1%;
The reacted gas of third stage catalytic deoxidation gets into interchanger E1, gets into steam boiler B3, gets into interchanger E2 cooling through pipeline 13 then through pipeline 12 again through pipeline 11; Divide dried up again; Gaseous tension 0.45Mpa after branch is dried up gets into pipeline 14, obtains 41850Nm
3/ h deoxidation gas (being product gas), wherein 26850Nm
3/ h is as the output of product gas, 15000Nm in addition
3/ h gets into pipeline 15 as returning gas; P is pressurized to 0.6MPa through compressor; Get into interchanger E1 heating through pipeline 16 again; Get into pipeline 1 through pipeline 17 then and mix, get into the first deoxidation reactor R1 (can move continuously according to above-mentioned technical process, realize continuing to produce) through pipeline 4 again with raw material coal-seam gas 0.
In the present embodiment, as the 15000Nm that returns gas
3/ h is compressed to 0.6MPa by pressure 0.45MPa, and compression power consumption is 229kWh only.
The catalytic deoxidation reaction process of present embodiment coal field coal-seam gas is as shown in Figure 3, adopts 4 stage reactors to carry out 4 grades of catalytic deoxidation reactions:
Coal field coal-seam gas (raw material coal-seam gas) consists of (vol%): CH
450, O
210.5, N
239.5.Tolerance is 30000Nm
3/ h, 120 ℃ of temperature, pressure 0.6MPa.
The raw material coal-seam gas is divided into four parts and (is respectively 4500Nm
3/ h, 6000Nm
3/ h, 9000Nm
3/ h and 10500Nm
3/ h) get into the first step, the second stage, the third stage and fourth stage reactor drum respectively:
The 4500Nm of first part
3/ h raw material coal-seam gas 0 gets into pipeline 1, with the 9000Nm from pipeline 21
3/ h (421 ℃ of temperature) returns gas to be mixed, and mixes O in the gas of back
2Content is 3.5%, and 330 ℃ of temperature get among the first step reactor drum R1 through pipeline 5, under catalyst action, carry out the reaction of first step catalytic deoxidation; Reacted gas gets into pipeline 6 from first step reactor drum R1 outlet, and the exit gas temperature is 630 ℃, wherein O
2＜0.1%; With water cooling and produce steam, the gas temperature behind the controlled chilling is 412 ℃ to this gas in steam boiler B1, gets into pipeline 7;
The 6000Nm of second section
3/ h raw material coal-seam gas 0 joins in the pipeline 7 through pipeline 2, mixes with reaction of first step catalytic deoxidation and cooled gas, and after the mixing, O
2Be 3.23%, 330 ℃ of temperature in pipeline 8 entering second stage reactor drum R2, under catalyst action, are carried out second stage catalytic deoxidation reaction; Reactor drum R2 outlet gets into pipeline 9,610 ℃ of exit gas temperatures, wherein O to reacted gas from the second stage
2＜0.1%; With water cooling and produce steam, the gas temperature behind the controlled chilling is 415 ℃ to this gas in steam boiler B2, gets into pipeline 10;
The 9000Nm of third part
3/ h raw material coal-seam gas 0 joins in the pipeline 10 through pipeline 3, mixes with reaction of second stage catalytic deoxidation and cooled gas, and after the mixing, O
2Be 3.32%, 330 ℃ of temperature get among the third stage reactor drum R3 through pipeline 11, under catalyst action, carry out the reaction of third stage catalytic deoxidation; Reacted gas gets into pipeline 12,617 ℃ of exit gas temperatures, wherein O from third stage reactor drum R3 outlet
2＜0.1%; With water cooling and produce steam, the gas temperature behind the controlled chilling is 399 ℃ to this gas in steam boiler B3, gets into pipeline 13;
Tetrameric 10500Nm
3/ h raw material coal-seam gas 0 joins in the pipeline 13 through pipeline 4, mixes with reaction of third stage catalytic deoxidation and cooled gas, and after the mixing, O
2Be 2.83%, 330 ℃ of temperature get among the fourth stage reactor drum R4 through pipeline 14, under catalyst action, carry out the reaction of fourth stage catalytic deoxidation; Reacted gas gets into pipeline 15,579 ℃ of exit gas temperatures, wherein O from fourth stage reactor drum R4 outlet
2＜0.1%;
The reacted gas of fourth stage catalytic deoxidation gets into interchanger E1, gets into steam boiler B4, gets into interchanger E2 cooling through pipeline 17 then through pipeline 16 again through pipeline 15; Divide dried up again; Gaseous tension 0.45Mpa after branch is dried up gets into pipeline 18, obtains 35800Nm
3/ h deoxidation gas (being product gas), wherein 26850Nm
3/ h is as the output of product gas, 9000Nm in addition
3/ h gets into pipeline 19 as returning gas; P is pressurized to 0.6MPa through compressor; Get into interchanger E1 heating through pipeline 20 again; Get into pipeline 1 through pipeline 21 then and mix, get into the first deoxidation reactor R1 (can move continuously according to above-mentioned technical process, realize continuing to produce) through pipeline 5 again with raw material coal-seam gas 0.
In the present embodiment, as the 9000Nm that returns gas
3/ h is compressed to 0.6MPa by pressure 0.45MPa, and compression power consumption is 137kWh only.
Comparative Examples 2
This example is the Comparative Examples of embodiment 4:
The raw material coal-seam gas is formed (vol%, down together): CH
435, O
213.6, N
251.4.Tolerance is 20000Nm
3/ h, deoxygenation adopts a reactor drum, and advancing the reactor drum oxygen concn is 3.5%, and then recycle ratio is 2.9, and promptly diluting tolerance is 58000Nm
3/ h, the pressure that advances deoxidation reactor is 0.3MPa, 330 ℃ of temperature.Go out 660 ℃ of temperature of reactor, O
2＜0.1%, pressure is 0.2MPa behind heat exchange refrigerated separation water.
Carrier gas is compressed to 0.3MPa from pressure 0.2MPa, compression power consumption 1246kWh.
The catalytic deoxidation reaction process of present embodiment coal field coal-seam gas is as shown in Figure 1, adopts 2 stage reactors to carry out 2 grades of catalytic deoxidation reactions:
Coal field coal-seam gas (raw material coal-seam gas) consists of (vol%): CH
435, O
213.6, N
251.4.Tolerance is 20000Nm
3/ h, 120 ℃ of temperature, pressure 0.3MPa.
The raw material coal-seam gas is divided into two portions and (is respectively 8400Nm
3/ h and 11600Nm
3/ h) get into the first step and second stage reactor drum respectively:
The 8400Nm of first part
3/ h raw material coal-seam gas 0 gets into pipeline 1, with the 25200Nm from pipeline 13
3/ h (393 ℃ of temperature) returns gas to be mixed, and mixes O in the gas of back
2Content is 3.34%, and 330 ℃ of temperature get among the first step reactor drum R1 through pipeline 3, under catalyst action, carry out the reaction of first step catalytic deoxidation; Reacted gas gets into pipeline 4 from first step reactor drum R1 outlet, and the exit gas temperature is 651 ℃, wherein O
2＜0.1%; With water cooling and produce steam, the gas temperature behind the controlled chilling is 395 ℃ to this gas in steam boiler B1, gets into pipeline 5;
The 11600Nm of second section
3/ h raw material coal-seam gas 0 joins in the pipeline 5 through pipeline 2, mixes with reaction of first step catalytic deoxidation and cooled gas, and after the mixing, O
2Be 3.5%, 330 ℃ of temperature in pipeline 6 entering second stage reactor drum R2, under catalyst action, are carried out second stage catalytic deoxidation reaction; Reactor drum R2 outlet gets into pipeline 7,660 ℃ of exit gas temperatures, wherein O to reacted gas from the second stage
2＜0.1%;
Catalytic deoxidation reacted gas in the second stage gets into interchanger E1, gets into steam boiler B2, gets into interchanger E2 cooling through pipeline 9 then through pipeline 8 again through pipeline 7; Divide dried up again; Gaseous tension 0.2Mpa after branch is dried up gets into pipeline 10, obtains 42400Nm
3/ h deoxidation gas (being product gas), wherein 17280Nm
3/ h is as the output of product gas, 25200Nm in addition
3/ h gets into pipeline 11 as returning gas; P is pressurized to 0.3MPa through compressor; Get into interchanger E1 heating through pipeline 12 again; Get into pipeline 1 through pipeline 13 then and mix, get into the first deoxidation reactor R1 (can move continuously according to above-mentioned technical process, realize continuing to produce) through pipeline 3 again with raw material coal-seam gas 0.
In the present embodiment, as the 25200Nm that returns gas
3/ h deoxidation gas is compressed to 0.3MPa by pressure 0.2MPa, and compression power consumption is 541kWh only.
More than in each stage reactor of each embodiment, it is embodiment 1 disclosed manganese deoxidier in 200610022255.3 the Chinese invention patent application that the dehydrogenation catalyst of employing is application number, that is:
Its weight percent is formed (is 100% with active ingredient, support carrier, sticker deal sum): MnO
240%, 4A molecular sieve 30%, attapulgite 30%, other has xylogen to account for MnO
2, 4A molecular sieve and attapulgite the mixture total weight amount 10%.
This manganese deoxidier makes through following method:
(1), with the MnO of said deal
2, 4A molecular sieve, attapulgite and xylogen mix, and is ground into the above powder of 300 orders;
(2), with (1) the powder roller forming in step;
(3), with the mixture behind (2) one-step forming 300～400 ℃ of following roastings 3～5 hours, promptly get.
Claims (3)
1. catalysis deoxidization process for coal bed gas of coal mine zone is characterized in that: adopt staged reactor to carry out multistage catalytic deoxidation reaction, control O in gasinlet temperature and the inlet gas of each stage reactor
2Content makes the Outlet Gas Temperature of each stage reactor of catalytic deoxidation reaction back equal≤660 ℃;
Adopt following method to control O in the inlet gas of each stage reactor
2Content≤3.5%:
(1) inlet gas of first step reactor drum control:
Adopt part deoxidation and cooled gas to join in the coal-seam gas of feed coal mining area, be diluted to wherein O as returning gas
2Content≤3.5%;
(2) inlet gas of other each stage reactor control:
Feed coal mining area coal-seam gas is joined in reaction of previous stage catalytic deoxidation and the cooled gas, make wherein O
2Content≤3.5%;
With the reacted gas of previous stage catalytic deoxidation with water cooling and produce steam; Rely on the gas temperature behind the controlled chilling to make its and the feed coal mining area mixed temperature of coal-seam gas reach 330 ℃ ± 10 ℃ of dehydrogenation catalyst starting temperatures, get into again and carry out catalytic deoxidation in the reactor drum of corresponding stage and react.
2. technology according to claim 1 is characterized in that: control O in the inlet gas of each stage reactor
2Content≤3.5%.
3. technology according to claim 1 is characterized in that: described staged reactor is the 2-4 stage reactor.
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Families Citing this family (13)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102433185A (en) * | 2010-09-29 | 2012-05-02 | 中国石油化工股份有限公司 | Catalytic deoxidation method for coalbed gas in coal mine area |
| CN102433184A (en) * | 2010-09-29 | 2012-05-02 | 中国石油化工股份有限公司 | Method for directly removing oxygen from coalbed gas by using hydrogen |
| CN102433181B (en) * | 2010-09-29 | 2014-03-12 | 中国石油化工股份有限公司 | Catalytic deoxidation method for coalbed gas in coal mine area |
| CN102433182A (en) * | 2010-09-29 | 2012-05-02 | 中国石油化工股份有限公司 | Catalytic deoxidation method for coalbed gas in coal mine area |
| CN102433183A (en) * | 2010-09-29 | 2012-05-02 | 中国石油化工股份有限公司 | Normal-temperature self-running deoxidation method for coalbed gas |
| CN102206521B (en) * | 2011-05-05 | 2013-06-05 | 西南化工研究设计院有限公司 | Dual-pressure catalytic deoxidation process of CMM (Coalbed Methane) in coal mine area |
| CN102533367B (en) * | 2011-12-23 | 2014-04-30 | 新地能源工程技术有限公司 | System and method for catalytic combustion deoxidation of methane gas |
| CN102719290B (en) * | 2012-05-03 | 2013-10-30 | 太原理工大学 | Two-stage fluidized bed coal bed gas non-catalytic deoxidation technology |
| CN102660343B (en) * | 2012-05-22 | 2013-08-07 | 太原理工大学 | Coal-bed gas non-catalytic deoxygenation process by utilizing dual-barrel moving-bed reactor |
| CN102839028B (en) * | 2012-09-18 | 2014-03-19 | 新地能源工程技术有限公司 | Energy-saving method of deoxidizing coalbed methane |
| CN103013606A (en) * | 2012-12-28 | 2013-04-03 | 张仕霖 | Biogas deoxidization technology |
| CN103160352B (en) * | 2013-03-11 | 2014-09-03 | 大连天元气体技术有限公司 | Oxygen-removal method of oxygen-containing coal-bed gas |
| CN103589471B (en) * | 2013-11-17 | 2015-01-07 | 北京科技大学 | Energy-saving device and process for low-temperature combustion deoxygenation of biogas |
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