CN221028288U - Coalbed methane separation system - Google Patents
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- CN221028288U CN221028288U CN202322560911.7U CN202322560911U CN221028288U CN 221028288 U CN221028288 U CN 221028288U CN 202322560911 U CN202322560911 U CN 202322560911U CN 221028288 U CN221028288 U CN 221028288U
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 98
- 238000000926 separation method Methods 0.000 title claims abstract description 16
- 238000005262 decarbonization Methods 0.000 claims abstract description 40
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 7
- 238000006297 dehydration reaction Methods 0.000 claims abstract description 6
- 230000023556 desulfurization Effects 0.000 claims abstract description 6
- 230000018044 dehydration Effects 0.000 claims abstract description 5
- 239000007788 liquid Substances 0.000 claims description 36
- 239000002253 acid Substances 0.000 claims description 23
- 238000010521 absorption reaction Methods 0.000 claims description 20
- 238000011069 regeneration method Methods 0.000 claims description 20
- 230000008929 regeneration Effects 0.000 claims description 19
- 229910052753 mercury Inorganic materials 0.000 claims description 9
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 claims description 8
- 239000007789 gas Substances 0.000 description 54
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 12
- 239000003245 coal Substances 0.000 description 11
- PVXVWWANJIWJOO-UHFFFAOYSA-N 1-(1,3-benzodioxol-5-yl)-N-ethylpropan-2-amine Chemical compound CCNC(C)CC1=CC=C2OCOC2=C1 PVXVWWANJIWJOO-UHFFFAOYSA-N 0.000 description 6
- QMMZSJPSPRTHGB-UHFFFAOYSA-N MDEA Natural products CC(C)CCCCC=CCC=CC(O)=O QMMZSJPSPRTHGB-UHFFFAOYSA-N 0.000 description 6
- 239000001569 carbon dioxide Substances 0.000 description 6
- 229910002092 carbon dioxide Inorganic materials 0.000 description 6
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 4
- 239000002245 particle Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000005065 mining Methods 0.000 description 2
- 239000003345 natural gas Substances 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 239000003507 refrigerant Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 101001121408 Homo sapiens L-amino-acid oxidase Proteins 0.000 description 1
- 102100026388 L-amino-acid oxidase Human genes 0.000 description 1
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- UBAZGMLMVVQSCD-UHFFFAOYSA-N carbon dioxide;molecular oxygen Chemical compound O=O.O=C=O UBAZGMLMVVQSCD-UHFFFAOYSA-N 0.000 description 1
- 239000013064 chemical raw material Substances 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 238000005261 decarburization Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000010881 fly ash Substances 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 239000011159 matrix material Substances 0.000 description 1
- 238000000034 method Methods 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000003303 reheating Methods 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
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Abstract
本实用新型公开了一种煤层气分离系统，涉及煤层气分离技术领域。包括依次连通的脱碳装置、脱碳气分离器、脱硫装置、脱水装置、脱汞装置、低温液化装置和输送管道，以及复热换热器、第一换热器、第一涡流管和第二涡流管。复热换热器的冷端分别与低温液化装置和输送管道连通，热端分别与第二涡流管和外界连通；第一换热器的热端分别与脱碳装置和脱碳气分离器连通，冷端分别与第一涡流管和外界连通。本实用新型通过涡流管向换热器提供冷源，向脱碳装置和复热换热器提供热源，使装置更加简洁化，并通过复热换热器，将液化的煤层气升温变为气体，进而便于在输送管道内运输，减少了运输的成本，提高了运输的安全性。
The utility model discloses a coalbed methane separation system, which relates to the technical field of coalbed methane separation. It includes a decarbonization device, a decarbonization gas separator, a desulfurization device, a dehydration device, a demercuration device, a low-temperature liquefaction device and a conveying pipeline, as well as a recuperation heat exchanger, a first heat exchanger, a first vortex tube and a second vortex tube, which are connected in sequence. The cold end of the recuperation heat exchanger is respectively connected to the low-temperature liquefaction device and the conveying pipeline, and the hot end is respectively connected to the second vortex tube and the outside world; the hot end of the first heat exchanger is respectively connected to the decarbonization device and the decarbonization gas separator, and the cold end is respectively connected to the first vortex tube and the outside world. The utility model provides a cold source to the heat exchanger through the vortex tube, and provides a heat source to the decarbonization device and the recuperation heat exchanger, so that the device is more concise, and the liquefied coalbed methane is heated and converted into gas through the recuperation heat exchanger, so as to facilitate transportation in the conveying pipeline, reduce the transportation cost, and improve the transportation safety.
Description
技术领域Technical Field
本实用新型涉及煤层气分离技术领域，特别涉及一种煤层气分离系统。The utility model relates to the technical field of coal bed gas separation, in particular to a coal bed gas separation system.
背景技术Background technique
煤层气是指赋存在煤层中，以甲烷为主要成分、以吸附在煤基质颗粒表面为主，并部分游离于煤孔隙中或溶解于煤层水中的天然气体，是煤的伴生矿产资源，属非常规天然气。煤层气可以用来发电，用作工业燃料、化工原料和居民生活燃料。煤层气随着煤炭的开采泄漏到大气中，会加剧全球的温室效应。在采煤之前先采出煤层气，煤矿生产中的瓦斯将降低70％～85％。Coalbed methane refers to natural gas that exists in coal seams, with methane as the main component, mainly adsorbed on the surface of coal matrix particles, and partially free in coal pores or dissolved in coal seam water. It is a mineral resource associated with coal and belongs to unconventional natural gas. Coalbed methane can be used for power generation, industrial fuel, chemical raw material and residential fuel. Coalbed methane leaks into the atmosphere with coal mining, which will aggravate the global greenhouse effect. If coalbed methane is extracted before coal mining, the gas in coal mine production will be reduced by 70% to 85%.
煤层气中主要成分是甲烷，还包含有一部分氧气、二氧化碳、氮气和硫化物等杂质，在使用前需要将这部分杂质脱除，以免降低煤层气的热值，增大煤层气保存和输送的能耗等。The main component of coalbed methane is methane, and it also contains some impurities such as oxygen, carbon dioxide, nitrogen and sulfide. These impurities need to be removed before use to avoid reducing the calorific value of coalbed methane and increasing the energy consumption of coalbed methane storage and transportation.
公告号为CN215855952U的专利公开了一种煤层气净化系统，包括吸收塔、LNG高压闪蒸罐、LNG低压闪蒸罐、贫富液换热器、再生塔、第一酸气分离器、脱碳气分离器、脱硫塔、干燥器、脱汞塔和粉尘过滤器，该专利能够有效地对煤气层进行脱酸、脱硫、脱汞、脱芳香烃和重烃的处理，但处理中由多个装置提供热源和冷源，不利于设备的维护，增加了生产的成本，并且最终产出的液化煤层气不利于在管道中运输，需要装罐后再运走，增加了运输成本的同时，还具有安全隐患。The patent with announcement number CN215855952U discloses a coalbed methane purification system, including an absorption tower, an LNG high-pressure flash tank, an LNG low-pressure flash tank, a lean-rich liquid heat exchanger, a regeneration tower, a first acid gas separator, a decarbonization gas separator, a desulfurization tower, a dryer, a demercuration tower and a dust filter. The patent can effectively deacidify, desulfurize, demercurate, remove aromatic hydrocarbons and heavy hydrocarbons from the coal gas layer, but multiple devices are used to provide heat and cold sources during the treatment, which is not conducive to equipment maintenance and increases production costs. The liquefied coalbed methane finally produced is not conducive to transportation in pipelines and needs to be canned before being transported, which increases transportation costs and also poses safety hazards.
实用新型内容Utility Model Content
本实用新型主要目的在提供一种煤层气分离系统，以解决上述问题。The main purpose of the utility model is to provide a coal bed gas separation system to solve the above problems.
为达上述目的，本实用新型提供一种煤层气分离系统，包括依次连通的脱碳装置、脱碳气分离器、脱硫装置、脱水装置、脱汞装置和低温液化装置，其特征在于，还包括复热换热器、第一换热器、第一涡流管、第二涡流管和用于输送煤层气的输送管道；To achieve the above-mentioned purpose, the utility model provides a coalbed methane separation system, comprising a decarbonization device, a decarbonization gas separator, a desulfurization device, a dehydration device, a demercuration device and a low-temperature liquefaction device connected in sequence, characterized in that it also comprises a recuperation heat exchanger, a first heat exchanger, a first vortex tube, a second vortex tube and a conveying pipeline for conveying coalbed methane;
所述复热换热器的冷端入口与低温液化装置的出口连通，冷端出口与输送管道连通，热端入口与所述第二涡流管的热气出口连通，热端出口与外界连通；The cold end inlet of the recuperation heat exchanger is connected to the outlet of the low-temperature liquefaction device, the cold end outlet is connected to the delivery pipeline, the hot end inlet is connected to the hot gas outlet of the second vortex tube, and the hot end outlet is connected to the outside;
所述第一换热器位于所述脱碳装置和所述脱碳气分离器之间，其中，所述第一换热器的热端入口与所述脱碳装置连通，热端出口与所述脱碳气分离器的入口连通，冷端入口与所述第一涡流管的冷气出口连通，冷端出口与外界连通；The first heat exchanger is located between the decarbonization device and the decarbonization gas separator, wherein the hot end inlet of the first heat exchanger is connected to the decarbonization device, the hot end outlet is connected to the inlet of the decarbonization gas separator, the cold end inlet is connected to the cold air outlet of the first vortex tube, and the cold end outlet is connected to the outside;
所述脱碳装置设置有气体入口。The decarbonization device is provided with a gas inlet.
进一步的，还包括旋风分离器，所述旋风分离器的气体入口用于通入煤层气，所述旋风分离器的气体出口与脱碳装置的气体入口连通。Furthermore, it also includes a cyclone separator, the gas inlet of the cyclone separator is used to introduce coalbed methane, and the gas outlet of the cyclone separator is connected to the gas inlet of the decarbonization device.
进一步的，所述脱汞装置和低温液化装置之间设置有预冷换热器，所述预冷换热器的热端入口与所述脱汞装置的出口连通，热端出口与所述低温液化装置的入口连通，冷端入口与所述第二涡流管的冷气出口连通，冷端出口与外界连通。Furthermore, a precooling heat exchanger is provided between the mercury removal device and the low-temperature liquefaction device, the hot end inlet of the precooling heat exchanger is connected to the outlet of the mercury removal device, the hot end outlet is connected to the inlet of the low-temperature liquefaction device, the cold end inlet is connected to the cold air outlet of the second vortex tube, and the cold end outlet is connected to the outside.
进一步的，所述脱碳装置包括吸收塔、闪蒸罐、再生塔、酸气分离器、第二换热器和用于向所述再生塔提供汽提再生热量的再沸器；Further, the decarbonization device includes an absorption tower, a flash tank, a regeneration tower, an acid gas separator, a second heat exchanger, and a reboiler for providing stripping regeneration heat to the regeneration tower;
所述气体入口设置于所述吸收塔底部，所述吸收塔底部另一侧设置有富液出口，上部设置有贫液入口，顶部设置有与所述第一换热器连通的煤层气出口；The gas inlet is arranged at the bottom of the absorption tower, a rich liquid outlet is arranged at the other side of the bottom of the absorption tower, a lean liquid inlet is arranged at the top, and a coalbed methane outlet connected to the first heat exchanger is arranged at the top;
所述再生塔底部设置有贫液出口，上部设置有富液入口，顶部设置有酸性气体出口；The regeneration tower is provided with a lean liquid outlet at the bottom, a rich liquid inlet at the top, and an acid gas outlet at the top;
所述闪蒸罐的一端与所述富液出口连通，另一端与所述富液入口连通；One end of the flash tank is connected to the rich liquid outlet, and the other end is connected to the rich liquid inlet;
所述第二换热器的热端入口与所述酸性气体出口连通，热端出口与酸气分离器的入口端连通，冷端入口与所述第二涡流管的冷气出口连通，冷端出口与外界连通；The hot end inlet of the second heat exchanger is connected to the acid gas outlet, the hot end outlet is connected to the inlet of the acid gas separator, the cold end inlet is connected to the cold gas outlet of the second vortex tube, and the cold end outlet is connected to the outside;
所述再沸器与第一涡流管的热气出口连通。The reboiler is communicated with the hot gas outlet of the first vortex tube.
进一步的，还包括第三换热器；所述第三换热器的冷端入口与所述第一涡流管的冷气出口连通，冷端出口与外界连通，热端入口与所述贫液出口连通，热端出口与所述贫液入口连通。Furthermore, it also includes a third heat exchanger; the cold end inlet of the third heat exchanger is connected to the cold air outlet of the first vortex tube, the cold end outlet is connected to the outside, the hot end inlet is connected to the lean liquid outlet, and the hot end outlet is connected to the lean liquid inlet.
进一步的，还包括火炬，所述火炬与所述酸气分离器的出口端连通。Furthermore, it also includes a torch, which is connected to the outlet end of the acid gas separator.
本实用新型具有以下有益效果：The utility model has the following beneficial effects:
本实用新型通过涡流管向各个换热器和再沸器提供冷源和热源，减少了提供冷源的装置数量，便于设备的维护；通过设置预冷换热器，使煤层气在低温液化前先降低了一定的温度，减少了低温液化时冷剂的消耗并保证了后续低温液化的效果；通过复热换热器，使液态的煤层气变为气态，方便了煤层气在管道内运输，降低了运输成本，提高了运输的安全性。The utility model provides cold source and heat source to each heat exchanger and reboiler through vortex tubes, reduces the number of devices providing cold source and facilitates equipment maintenance; by arranging a pre-cooling heat exchanger, the temperature of the coalbed methane is lowered to a certain extent before low-temperature liquefaction, reduces the consumption of refrigerant during low-temperature liquefaction and ensures the effect of subsequent low-temperature liquefaction; through the reheating heat exchanger, the liquid coalbed methane is converted into gaseous state, which facilitates the transportation of the coalbed methane in the pipeline, reduces the transportation cost and improves the safety of transportation.
附图说明BRIEF DESCRIPTION OF THE DRAWINGS
图1为本实用新型提出的一种煤层气分离系统的示意图；FIG1 is a schematic diagram of a coalbed methane separation system proposed by the present invention;
图中：1-吸收塔；2-再生塔；3-脱碳气分离器；4-脱硫装置；5-脱水装置；6-脱汞装置；7-低温液化装置；8-复热换热器；9-第一换热器；10-第二换热器；11-第三换热器；12-涡流管；13-火炬；14-预冷换热器；15-酸气分离器；16-第二涡流管；101-闪蒸罐。In the figure: 1-absorption tower; 2-regeneration tower; 3-decarbonization gas separator; 4-desulfurization device; 5-dehydration device; 6-mercury removal device; 7-low-temperature liquefaction device; 8-reheat heat exchanger; 9-first heat exchanger; 10-second heat exchanger; 11-third heat exchanger; 12-vortex tube; 13-flare; 14-precooling heat exchanger; 15-acid gas separator; 16-second vortex tube; 101-flash tank.
具体实施方式Detailed ways
为达成上述目的及功效，本实用新型所采用的技术手段及构造，结合附图就本实用新型较佳实施例详加说明其特征与功能。In order to achieve the above-mentioned purpose and effect, the technical means and structure adopted by the utility model are described in detail with reference to the accompanying drawings for the preferred embodiments of the utility model and their features and functions.
如附图1所示，本实用新型中提供了一种煤层气分离系统，包括依次连通的脱碳装置、脱碳气分离器3、脱硫装置4、脱水装置5、脱汞装置6和低温液化装置7，其特征在于，还包括复热换热器8、第一换热器9、第一涡流管12、第二涡流管16和用于输送煤层气的输送管道；As shown in FIG. 1 , the utility model provides a coalbed methane separation system, comprising a decarbonization device, a decarbonization gas separator 3, a desulfurization device 4, a dehydration device 5, a demercuration device 6 and a low-temperature liquefaction device 7 connected in sequence, characterized in that it also comprises a recuperation heat exchanger 8, a first heat exchanger 9, a first vortex tube 12, a second vortex tube 16 and a conveying pipeline for conveying coalbed methane;
复热换热器8的冷端入口与低温液化装置7的出口连通，冷端出口与输送管道连通，热端入口与第二涡流管16的热气出口连通，热端出口与外界连通；The cold end inlet of the recuperation heat exchanger 8 is connected to the outlet of the cryogenic liquefaction device 7, the cold end outlet is connected to the delivery pipeline, the hot end inlet is connected to the hot gas outlet of the second vortex tube 16, and the hot end outlet is connected to the outside;
第一换热器9位于所述脱碳装置和所述脱碳气分离器3之间，其中，第一换热器9的热端入口与脱碳装置连通，热端出口与所述脱碳气分离器3的入口连通，冷端入口与第一涡流管12的冷气出口连通，冷端出口与外界连通；The first heat exchanger 9 is located between the decarbonization device and the decarbonization gas separator 3, wherein the hot end inlet of the first heat exchanger 9 is connected to the decarbonization device, the hot end outlet is connected to the inlet of the decarbonization gas separator 3, the cold end inlet is connected to the cold air outlet of the first vortex tube 12, and the cold end outlet is connected to the outside;
脱碳装置设置有气体入口。The decarburization device is provided with a gas inlet.
在实际使用中，用空压机向第一涡流管12和第二涡流管16的进气口通入气体，将被压缩的煤层气从脱碳装置的气体入口进入脱碳装置，脱除部分二氧化碳和硫化氢，并从脱碳装置中的煤层气出口排出，排出的煤层气经第一换热器9与第一涡流管12排出的冷气换热，降温至≤40℃后在脱碳气分离器3中进一步脱除二氧化碳，经脱碳处理后的煤层气中二氧化碳含量小于50ppmV，然后再依次通过用于脱除硫化氢的脱硫装置4、用于脱除水分的脱水装置5、用于脱除汞的脱汞装置6和用于将煤层气低温液化来脱除芳香烃和重烃的低温液化装置7。In actual use, an air compressor is used to introduce gas into the air inlet of the first vortex tube 12 and the second vortex tube 16, and the compressed coalbed methane enters the decarbonization device from the gas inlet of the decarbonization device, removes part of the carbon dioxide and hydrogen sulfide, and is discharged from the coalbed methane outlet in the decarbonization device. The discharged coalbed methane is heat exchanged with the cold air discharged from the first vortex tube 12 through the first heat exchanger 9, and is further removed from the carbon dioxide in the decarbonization gas separator 3 after being cooled to ≤40°C. The carbon dioxide content in the coalbed methane after decarbonization treatment is less than 50ppmV, and then passes through the desulfurization device 4 for removing hydrogen sulfide, the dehydration device 5 for removing water, the demercuration device 6 for removing mercury, and the low-temperature liquefaction device 7 for low-temperature liquefying the coalbed methane to remove aromatic hydrocarbons and heavy hydrocarbons.
从低温液化装置7离开的低温液态煤层气通过复热换热器8与第二涡流管16排出的热气换热，重新恢复为气态，接着进入输送管道输送至目的地。The low-temperature liquid coalbed methane leaving the low-temperature liquefaction device 7 exchanges heat with the hot gas discharged from the second vortex tube 16 through the recuperation heat exchanger 8, recovers to the gaseous state, and then enters the transmission pipeline for transportation to the destination.
在本实施例中，为避免煤层气携带粉煤灰，泥土等杂物进入系统，造成系统的堵塞与损伤，在煤层气进入脱碳装置前，使原料气先穿过过滤网，过滤出较大的颗粒，再进入旋风分离器，分离出剩下颗粒较小的杂物，最后使清洁的原料气进入脱碳装置，进行后续的分离步骤。In this embodiment, in order to prevent coalbed methane from carrying fly ash, soil and other debris into the system, causing blockage and damage to the system, before the coalbed methane enters the decarbonization device, the raw gas first passes through a filter to filter out larger particles, and then enters a cyclone separator to separate out the remaining smaller particles. Finally, the clean raw gas enters the decarbonization device for subsequent separation steps.
在本实施例中，脱汞装置6和低温液化装置7之间设置有预冷换热器14，预冷换热器14热端入口与脱汞装置6的出口连通，热端出口与低温液化装置7的入口连通，冷端入口与第二涡流管16的冷气出口连接，冷端出口与外界连通，以此来对即将进入低温液化装置7的煤层气进行预冷，保证后续低温液化的效果，并减少冷剂的消耗。In this embodiment, a precooling heat exchanger 14 is provided between the mercury removal device 6 and the cryogenic liquefaction device 7. The hot end inlet of the precooling heat exchanger 14 is connected to the outlet of the mercury removal device 6, the hot end outlet is connected to the inlet of the cryogenic liquefaction device 7, the cold end inlet is connected to the cold air outlet of the second vortex tube 16, and the cold end outlet is connected to the outside, so as to precool the coalbed methane that is about to enter the cryogenic liquefaction device 7, ensure the effect of subsequent cryogenic liquefaction, and reduce the consumption of refrigerant.
在本实施例中，脱碳装置包括吸收塔1、闪蒸罐101、再生塔2、酸气分离器15、火炬13、第二换热器10和用于向再生塔2提供汽提再生时热量的再沸器；气体入口设置于吸收塔1底部，吸收塔1底部另一侧设置有富液出口，上部设置有贫液入口，顶部设置有与第一换热器9连通的煤层气出口；再生塔2底部设置有贫液出口，上部设置有富液入口，顶部设置有酸性气体出口；闪蒸罐101一端与富液出口连通，另一端与富液入口连通；第二换热器10热端入口与酸性气体出口连通，热端出口与酸气分离器15连通，冷端入口与第二涡流管16的冷气出口连通，冷端出口与外界连通；再沸器与第一涡流管12的热气出口连通；火炬13与酸气分离器15的出口端连通；In this embodiment, the decarbonization device includes an absorption tower 1, a flash tank 101, a regeneration tower 2, an acid gas separator 15, a flare 13, a second heat exchanger 10 and a reboiler for providing heat for stripping regeneration to the regeneration tower 2; a gas inlet is arranged at the bottom of the absorption tower 1, a rich liquid outlet is arranged on the other side of the bottom of the absorption tower 1, a lean liquid inlet is arranged on the upper part, and a coalbed methane outlet connected to the first heat exchanger 9 is arranged on the top; a lean liquid outlet is arranged at the bottom of the regeneration tower 2, a rich liquid inlet is arranged on the upper part, and an acid gas outlet is arranged on the top; one end of the flash tank 101 is connected to the rich liquid outlet, and the other end is connected to the rich liquid inlet; the hot end inlet of the second heat exchanger 10 is connected to the acid gas outlet, the hot end outlet is connected to the acid gas separator 15, the cold end inlet is connected to the cold gas outlet of the second vortex tube 16, and the cold end outlet is connected to the outside; the reboiler is connected to the hot gas outlet of the first vortex tube 12; the flare 13 is connected to the outlet end of the acid gas separator 15;
煤层气从吸收塔1底部的气体入口进入吸收塔1，自下而上向吸收塔1顶部的煤层气出口移动，途中与吸收塔1上部贫液出口喷出的MDEA溶液(贫液)接触，MDEA溶液(贫液)会吸收气体中的部分硫化氢和二氧化碳，剩余的气体吸收了溶液的部分热量从吸收塔1顶部的煤层气出口排出；The coalbed methane enters the absorption tower 1 from the gas inlet at the bottom of the absorption tower 1, and moves from bottom to top to the coalbed methane outlet at the top of the absorption tower 1. On the way, it contacts the MDEA solution (lean liquid) sprayed from the lean liquid outlet at the top of the absorption tower 1. The MDEA solution (lean liquid) absorbs part of the hydrogen sulfide and carbon dioxide in the gas, and the remaining gas absorbs part of the heat of the solution and is discharged from the coalbed methane outlet at the top of the absorption tower 1.
吸收塔1中吸收了硫化氢和二氧化碳的MDEA溶液(富液)从富液出口离开吸收塔，进入闪蒸罐101中闪蒸，闪蒸出的闪蒸汽排至界外燃料气系统，闪蒸后的MDEA溶液(富液)从上部进入由富液入口进入再生塔2，在再生塔2中经汽提再生(再生时的热源由与再沸器连通的第一涡流管12的热气出口提供，再生时的温度为105℃～120℃)，脱除二氧化碳等酸性气体，脱除出的酸性气体(温度约95-100℃)由再生塔2顶部酸性气体出口排出，经第二换热器10与第二涡流管16排出的冷气换热，降温到40℃以下后进入酸气分离器15脱除部分酸气，脱除部分酸气的剩余气体进入火炬13，进而被引至高空排出。The MDEA solution (rich liquid) having absorbed hydrogen sulfide and carbon dioxide in the absorption tower 1 leaves the absorption tower from the rich liquid outlet, enters the flash tank 101 for flash evaporation, and the flash steam is discharged to the off-site fuel gas system. The flashed MDEA solution (rich liquid) enters the regeneration tower 2 from the top through the rich liquid inlet, and is regenerated by stripping in the regeneration tower 2 (the heat source during regeneration is provided by the hot gas outlet of the first vortex tube 12 connected to the reboiler, and the temperature during regeneration is 105° C. to 120° C.), and the acid gases such as carbon dioxide are removed. The removed acid gases (temperature of about 95-100° C.) are discharged from the acid gas outlet at the top of the regeneration tower 2, and are heat exchanged with the cold air discharged from the second vortex tube 16 through the second heat exchanger 10, and after cooling to below 40° C., enter the acid gas separator 15 to remove part of the acid gas. The remaining gas after the removal of part of the acid gas enters the flare 13 and is then led to high altitude for discharge.
再生后的MDEA溶液(贫液)由再生塔2底部的贫液出口排出，通过与贫液出口连通的贫液入口进入吸收塔1中，进行循环使用。The regenerated MDEA solution (lean solution) is discharged from the lean solution outlet at the bottom of the regeneration tower 2, and enters the absorption tower 1 through the lean solution inlet connected to the lean solution outlet for recycling.
在本实施例中，脱碳装置还包括第三换热器11；第三换热器11冷端入口与第一涡流管12的冷气出口连通，冷端出口与外界连通，热端入口与贫液出口连通，热端出口与贫液入口连通；从而使从贫液出口排出的MDEA溶液(贫液)经第三换热器11与第一涡流管12排出的冷气换热，降温至约45℃后进入吸收塔1中，以便于后续的循环使用。In this embodiment, the decarbonization device also includes a third heat exchanger 11; the cold end inlet of the third heat exchanger 11 is connected to the cold air outlet of the first vortex tube 12, the cold end outlet is connected to the outside, the hot end inlet is connected to the lean liquid outlet, and the hot end outlet is connected to the lean liquid inlet; so that the MDEA solution (lean liquid) discharged from the lean liquid outlet is heat exchanged with the cold air discharged from the first vortex tube 12 through the third heat exchanger 11, cooled to about 45°C and then enters the absorption tower 1 for subsequent recycling.
以上所述仅为本实用新型较佳实施例而已，非全部实施例，任何人应该得知在本实用新型的启示下做出的结构变化，凡是与本实用新型具有相同或者相近似的技术方案，均属于本实用新型的保护范围。The above description is only the preferred embodiment of the utility model, not all embodiments. Anyone should be aware that the structural changes made under the inspiration of the utility model, and all technical solutions that are the same or similar to the utility model, belong to the protection scope of the utility model.
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