CN100478317C - Technology of low temperature separation and concentration coal layer gas to produce methane - Google Patents
Technology of low temperature separation and concentration coal layer gas to produce methane Download PDFInfo
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- CN100478317C CN100478317C CN 200410040155 CN200410040155A CN100478317C CN 100478317 C CN100478317 C CN 100478317C CN 200410040155 CN200410040155 CN 200410040155 CN 200410040155 A CN200410040155 A CN 200410040155A CN 100478317 C CN100478317 C CN 100478317C
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Abstract
A process for low-temp separation of methane from coal seam gas and concentrating it includes such steps as removing O2, pressurizing, desulfurizing, decarbonizing, drying. Low-temp separation to obtain liquid methane, flowing in the condenser on the tower top for using it as the cold source of condensing reflux, and flowing the evaporated methane through heat exchanger to obtain product. Its purity is 95-99%. Its recovery rate is 95-99%.
Description
The invention belongs to gas separation technique field, especially adopt the technical process of cryogenic rectification method separating and concentrating gas.
Background technology
Coal-seam gas (CMM---coal mine mash gas) is the gas that is rich in methane, and methane concentration is more than 40%, and Gao Zheke reaches more than 80%.Usually can be directly as domestic fuel and generating, if will must bring up to methane concentration more than 95% as Application in Chemical Engineering or as automobile fuel.Because the domestic fuel usage quantity is limited, many coal-seam gas fail well to be utilized, and have not only caused the ample resources waste, also cause environmental pollution, have increased the weight of Greenhouse effect.For making full use of this resource of coal-seam gas (CMM), must carry the methane in the coal-seam gas dense to more than 95%.Owing to contain components such as air in the coal-seam gas, for safety, before concentrating, to oxygen be removed, can adopt catalytic deoxidation technology, the coal-seam gas that has also contains a small amount of sulphur, and also necessary desulfurization could guarantee follow-up concentration technology enforcement like this.
Coal-seam gas (CMM) is carried and densely can be adopted pressure swing adsorption process, and Southwest Chemical Research and Design Institute has been invented transformation absorption (PSA) and put forward dense methane technology (patent No. CN85103557B), and this method technology is simple, and maintenance cost is lower.The present invention is that to adopt low temperature method that coal-seam gas is carried dense, and its major advantage is a product methane purity height, can reach more than 95%, and yield is decided on the methane concentration in product purity and the coal-seam gas up to more than the 95%-99%.
The separation of coal-seam gas (CMM) mainly is a nitrogen and the separating of methane, it mainly is the boiling-point difference that utilizes nitrogen and methane that cryogenic rectification method separates, depress at standard atmosphere, the boiling point of nitrogen is 77.35K, and the boiling point of methane is 111.7K, both differ 34K, are easily that the two is isolating so adopt cryogenic rectification method, and key is the configuration of technical process.
The processing method of low ternperature separation process mainly adopts Fig. 1 and flow process shown in Figure 3 at present, through desulfurization, deoxygenation, decarburization and the dried coal-seam gas FC that contains 65% methane, pressure 3.5-5.0MPa, enter interchanger E1 precooling by pipeline 1, enter pipeline 2 after going out E1, enter reboiler E2 then to pipeline 3, its temperature out is than the high about 4K of tower still temperature, by throttling valve J1, pipeline 4 enters knockout tower T1.The knockout tower working pressure is 1.7-2.2MPa.By the low temperature fractionation effect of rectifying tower, the tower still obtains the liquid methane of 95%-99%, is throttled to 0.15MPa by pipeline 5 through throttling valve J2, goes into overhead condenser as low-temperature receiver through pipeline 6.The methane of evaporation enters interchanger E1 re-heat after pipeline 8 is discharged as product gas PM through pipeline 7.Rectifying tower top is given up nitrogen (containing methane＜5%) by pipeline 9, and throttling valve J3 is throttled to 0.15MPa, passes through pipeline 10 again, after interchanger E1 re-heat, discharges as useless nitrogen (WN) through pipeline 11.This technology is mainly used in the separation process of the coal-seam gas (CMM) of high methane concentration (more than 65%), when the coal-seam gas methane concentration is low, obtain the methane product of purity more than 95%, the steam output that reboiler is depended merely on the heating of raw material coal-seam gas can not satisfy the needed reflux ratio requirement of rectifying, therefore can not get content in the methane product more than 95%.
Above shortcoming in view of prior art the objective of the invention is to design a kind of technology, makes it to overcome the above shortcoming of the technology of being limited to, and the coal-seam gas of hanging down methane content can be proposed dense separation and obtain the methane product of purity more than 95%.
Summary of the invention
The coal-seam gas low ternperature separation process is carried dense methane technology, will carry out low ternperature separation process through deoxygenation, pressurization, desulfurization, decarburization, dried methane coal-seam gas, to obtain product methane.The tower still obtains the liquid methane of 95%-99% purity, the low-temperature receiver of overhead condenser as condensing reflux gone in throttling, the methane of evaporation is discharged as product after interchanger reclaims the cold re-heat, in the low ternperature separation process operation the one steam output auxiliary circulation that is used to improve the reboiler of low temperature separation unit is set, the methane that returns by condenser and by the external world mend into additional methane after compression, enter the interchanger cooling, then by entering the reboiler of rectifying tower, as the evaporation thermal source; And methane itself is further cooled, go out behind the reboiler by throttling overhead condenser as tower in the low-temperature receiver of rising vapor condensation.
Adopt technology of the present invention, under the liquid methane temperature, will contain the coal-seam gas of methane more than 45%, put forward dense purity to 95%-99%, methane recovery is greater than 95%.
Description of drawings:
Fig. 1 is the process flow diagram of prior art.
Fig. 2 is a process flow diagram of the present invention.
Fig. 3 is the process flow sheet of prior art.
Fig. 4 is the process flow sheet of the embodiment of the invention.
Embodiment
Can see by Fig. 2, the present invention is provided with a steam output auxiliary circulation that is used to improve the reboiler of low temperature separation unit in the low ternperature separation process operation, return methane and by the external world mend into additional methane after compression, enter the interchanger cooling, then by entering the reboiler of rectifying tower, as the evaporation thermal source; And methane itself is further cooled, and goes out to feed behind the reboiler low-temperature receiver of throttling column overhead condenser as rising vapor condensation in the tower.
Concrete technical process can be shown that E1, E4, E6 are interchanger by Fig. 4, and E2, E5 are reboiler, and E3 is a condenser, and T1 is a low-temperature fractionating tower, and P1 is a compressor, and EXP1 is a decompressor.With Fig. 3 relatively, wherein increased an auxiliary circulation, by compressor P1, reboiler and interchanger E6, reboiler E5, and condenser E3 forms, be mainly used in the steam output of raising tower still.This is because when the coal-seam gas methane concentration is low, when obtaining the methane product of purity more than 95%, reboiler is depended merely on the heating of raw material coal-seam gas, its steam output can not satisfy the needed reflux ratio requirement of rectifying, and can not get content in the methane product more than 95%, be the auxiliary circulation system of working medium so will increase by one with product gas.Also increased a decompressor EXP1 in the present embodiment, because the nitrogen content height in the coal-seam gas, exhausted air quantity is big, and the pressure height utilizes its expansion can produce cold, except that satisfying the needs of device own, also can produce a part of liquid methane product.The actual process process is like this, through desulfurization, deoxygenation, decarburization and the dried methane coal-seam gas of (surplus) more than 45% that contains in nitrogen, pressure 3.0-4.5MPa, enter interchanger E1 precooling through pipeline 1, pass through pipeline 2 again, enter tower still reboiler E2 as thermal source, tower bottoms heated make its evaporation, itself obtain simultaneously cooling, go out to enter interchanger E4 by pipeline 3 behind the tower still reboiler E2 and further enter pipeline 4 after the cooling, enter the low ternperature separation process tower of rectifying tower T1 by throttling valve J1, pipeline 16.The working pressure of T1 tower is 1.7-2.2MPa.Coal-seam gas in rectifying tower by the low temperature fractionation effect, the tower still obtains the liquid methane of purity more than 95%, liquid methane is gone into overhead condenser E3 as low-temperature receiver by pipeline 5, throttling valve J2, pipeline 6, make the vapor condensation that rises in the tower and reflux, the methane of evaporation enters interchanger E4 through pipeline 7 and cools off coal-seam gas into tower, go out to enter behind the interchanger E4 pipeline 15 and interchanger E1 precooling coal-seam gas and re-heat is discharged as product gas through pipeline 8.The useless nitrogen of cat head enters interchanger E4 by pipeline 9 and is heated to 155-165K, by pipeline 10 to decompressor EXP1, expand into 0.5-0.6MPa, useless nitrogen temperature is dropped to about 120K, by pipeline 12, throttling valve J3, pressure enters interchanger E4, pipeline 14 and interchanger E1 recovery cold by pipeline 13 after being reduced to 0.15MPa, is discharged by pipeline 11 after the re-heat.For auxiliary circulation, by after the returning methane and the additional methane by pipeline 17 and in compressor P1, be pressurized to 1.9-2.4MPa of pipeline 23, enter interchanger E6 cooling by pipeline 18, enter the reboiler E5 of rectifying tower T1 then by pipeline 19, as the evaporation thermal source, and itself is further cooled, and is throttled to 0.15MPa by pipeline 20, throttling valve J4 after going out reboiler E5, goes into the low-temperature receiver of throttling column overhead condenser E3 as rising vapor condensation in the tower through pipeline 21 again.The methane of evaporation enters compressor P1 by pipeline 23 after passing through pipeline 22 and interchanger E6 re-heat again.
Coal-seam gas after desulfurization, deoxygenation, decarburization, drying (dewatering) is formed CH
450% (surplus is N
2).Raw gas pressure 4.0MPa (g), knockout tower pressure 2.0MPa (g).The product methane concentration is 99% (the surplus N of being
2), yield 95%.Nitrogen content is greater than 95% in the useless nitrogen of cat head.It is 139K that unstripped gas is gone into the tower temperature, and tower still temperature is 164K, tower top temperature＜122K.Auxiliary circulation pressure is 2.4MPa (g), and internal circulating load is about 30% of material gas quantity.The expander inlet temperature is 163K, and the back pressure that expands is 0.5MPa (g), and temperature out is 127K.
Coal-seam gas after desulfurization, deoxygenation, decarburization, drying (dewatering) is formed CH
456% (surplus is N
2).Raw gas pressure 4.0MPa (g), knockout tower pressure 2.0MPa (g).The product methane concentration is 95% (the surplus N of being
2), yield＞97%.It is 140K that unstripped gas is gone into the tower temperature, and tower still temperature is 155K, tower top temperature 120K.Auxiliary circulation pressure is 2.4MPa (g), and internal circulating load is about 10% of material gas quantity.The expander inlet temperature is 154K, and the back pressure that expands is 0.5MPa (g), and temperature out is 119K.
Claims (3)
1, the coal-seam gas low ternperature separation process is carried dense methane technology, to carry out low ternperature separation process through deoxygenation, pressurization, desulfurization, decarburization and dried methane coal-seam gas, product methane with the purity that obtains 95%-99%, described methane coal-seam gas is cooled off by interchanger, and the reboiler that enters rectifying tower further cools off the knockout tower that rectifying tower is gone in throttling; The useless nitrogen of rectifying tower cat head gives off outside the device after interchanger reclaims the cold re-heat; The tower still obtains the liquid methane of 95%-99% purity, the low-temperature receiver of overhead condenser as condensing reflux gone in throttling, the methane of evaporation is discharged as product after interchanger reclaims the cold re-heat, it is characterized in that, in the low ternperature separation process operation the one steam output auxiliary circulation that is used to improve the reboiler of low temperature separation unit is set, the methane that returns by condenser and by the external world mend into additional methane after compression, enter the interchanger cooling, then by entering the reboiler of rectifying tower, as the evaporation thermal source; And methane itself is further cooled, go out behind the reboiler by throttling overhead condenser as tower in the low-temperature receiver of rising vapour condensation.
2, carry dense methane technology according to the described coal-seam gas low ternperature separation process of claim 1, it is characterized in that coal-seam gas is pressurized to 3.0-4.5MPa, the rectifying tower working pressure is 1.7-2.2MPa; The auxiliary circulation system pressure is higher than rectifying tower pressure 0.2-0.4MPa.
3, carry dense methane technology according to claim 1 or 2 described coal-seam gas low ternperature separation process, it is characterized in that, low temperature separation unit is provided with useless nitrogen expansive working operation.
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| CN 200410040155 CN100478317C (en) | 2004-07-09 | 2004-07-09 | Technology of low temperature separation and concentration coal layer gas to produce methane |
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Cited By (1)
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| CN101899342A (en) * | 2010-08-04 | 2010-12-01 | 西南化工研究设计院 | Process for producing liquefied natural gas by coal bed gas in mine coal |
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| CN101096606B (en) * | 2006-06-27 | 2011-06-15 | 上海标氢气体技术有限公司 | Coal mine mash gas low-pressure concentration method |
| CN101096907B (en) * | 2006-06-27 | 2012-02-01 | 上海汉兴能源科技有限公司 | Method for producing natural gas from coal bed gas under low pressure |
| CN100404988C (en) * | 2006-07-03 | 2008-07-23 | 中国科学院理化技术研究所 | Air-contained coal gas gasification and separation process and equipment |
| KR20090068213A (en) * | 2006-08-23 | 2009-06-25 | 쉘 인터내셔날 리써취 마트샤피지 비.브이. | Method and apparatus for treating a hydrocarbon stream |
| CN101531560B (en) * | 2008-03-13 | 2013-01-23 | 中国科学院理化技术研究所 | Method for extracting methane from oxygen-containing coal-bed gas through low-temperature liquefying separation |
| CN101818984B (en) * | 2010-04-21 | 2012-05-30 | 中国石油大学(北京) | Full liquefying separation process for air-containing coal bed gas |
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| CN102767936A (en) * | 2012-07-18 | 2012-11-07 | 重庆耐德工业股份有限公司 | Process for producing gas-phase natural gas and liquid-phase natural gas through nitrogen-methane separation in nitrogen-containing natural gas |
| CN103055532B (en) * | 2012-12-06 | 2015-08-12 | 江苏三木集团有限公司 | Polyalcohol acrylate reclaims the device of cyclohexane in producing |
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| CN104194853B (en) * | 2014-07-04 | 2016-06-15 | 韩俊义 | The device of the coalbed methane containing oxygen synthesis LNG of a kind of methane content 15-40% and technique |
| CN105296038A (en) * | 2015-11-27 | 2016-02-03 | 中煤科工集团重庆研究院有限公司 | Oxygen-bearing coal-bed gas low-temperature concentration method and device for implementing method |
| CN105605883A (en) * | 2016-03-25 | 2016-05-25 | 北京中科瑞奥能源科技股份有限公司 | Oxygen-bearing coalbed methane liquefaction separation system and technique |
| CN105972935B (en) * | 2016-05-04 | 2018-06-05 | 中煤科工集团重庆研究院有限公司 | A kind of method of coalbed methane containing oxygen separation of methane |
| CN105890282B (en) * | 2016-05-04 | 2018-06-05 | 中煤科工集团重庆研究院有限公司 | A kind of device of coalbed methane containing oxygen separation of methane |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101899342A (en) * | 2010-08-04 | 2010-12-01 | 西南化工研究设计院 | Process for producing liquefied natural gas by coal bed gas in mine coal |
| CN101899342B (en) * | 2010-08-04 | 2012-12-26 | 西南化工研究设计院有限公司 | Process for producing liquefied natural gas by coal bed gas in mine coal |
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