CN204569865U - Single stage method coal synthetic natural gas system - Google Patents
Single stage method coal synthetic natural gas system Download PDFInfo
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- CN204569865U CN204569865U CN201520257691.3U CN201520257691U CN204569865U CN 204569865 U CN204569865 U CN 204569865U CN 201520257691 U CN201520257691 U CN 201520257691U CN 204569865 U CN204569865 U CN 204569865U
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Abstract
The utility model discloses single stage method coal synthetic natural gas system, comprise the first absorption tower of the low temperature washing device for methanol connected successively, the shell side of the first feed gas heater or tube side, deep purifying devulcanizer, the tube side of the second feed gas heater or shell side, isothermal methanation reactor, the tube side of the first feed gas heater or shell side, the shell side of feedwater preheater or the second absorption tower of tube side, demineralized-water preheater, condensate separator and low temperature washing device for methanol; Wherein the shell side of the second feed gas heater or tube side outlet are also connected with the import of isothermal methanation reactor through the shell side of adiabatic methanator, vapor superheater or tube side successively; The outlet of described isothermal methanation reactor is also connected with the import of adiabatic methanation reactor through the tube side of the second feed gas heater or shell side, recycle gas compressor successively.The utility model structure is simple, short flow, plant running and cost of investment are low, centralized recovery heat energy by-product high-quality steam.
Description
Technical field
The utility model relates to a kind of synthetic natural gas system, specifically a kind of single stage method coal synthetic natural gas system.
Background technology
Along with constantly increasing the weight of of current haze, improving constantly of environmental requirement, energy-conservation, reduce discharging, consumption reduction becomes the study hotspot of current coal chemical technology.Clean as one, the efficient energy product of Sweet natural gas are more and more subject to people's attention.The demand of domestic natural gas grew with each passing day in recent years.In order to meet the demand of domestic current natural gas, government is positive from external inlet natural gas on the one hand, on the one hand according to the energy structure of China's " oil starvation, weak breath, rich coal ", and develop actively coal preparing natural gas (SNG) industry, realize the conversion on the spot of coal, reduce transportation cost.Guarantee the energy security of China as Strategic Technology deposit simultaneously.
Traditional coal preparing natural gas flow process is that the raw gas produced by gasification is adjusted to suitable H through CO changing device successively
2with the ratio of CO, remove after sour gas and other impurity through low temperature washing device for methanol again, qualified purified gas generates the synthetic natural gas meeting national Natural gas standard and require through methanation reaction, then after natural gas compressing, Sweet natural gas drying, enter Gao Long-distance Transmission Pipeline.
In traditional coal preparing natural gas flow process, main heat releasing unit comprises CO changing device and methanation device, and wherein transformationreation principal reaction principle is as follows:
Methanation principal reaction principle is as follows:
From Technological Economy aspect, traditional coal preparing natural gas project is due to technical process long (comprising multiple flow process such as CO conversion, removal of impurities de-carbon, methanation reaction), high temperature service pipeline many (adiabatic main methanator temperature out is up to 620 DEG C), cause selection difficulty, invest high, and CO changing device and methanation device all release amount of heat, heat release disperses, and cause low-grade remaining heat on the high side, heat recovery efficiency cost is high.
In addition, CO transformationreation and methanation reaction are all strong exothermal reactions, can reach molecular balance very soon, and in adiabatic reactor, the temperature of reactor and beds can raise rapidly.Adiabatic reaction flow process is converted, in order to avoid overtemperature must add steam temperature control for CO; For methanation adiabatic reaction flow process, in order to avoid temperature runaway appears in catalyzer high temperature sintering and runaway reaction, generally return one synthetic gas by circulation and to mix the CO concentration reduced into reactor with unstripped gas and control the temperature that methanator exports.According to chemical equilibrium theory, the too high transformation efficiency limiting CO of reaction temperature out.In order to improve the transformation efficiency of CO, guarantee the CH in synthetic gas
4concentration is up to standard, needs at follow-up series connection two-stage low temperature methanator.For this flow process, high-temperature methanation equipment is many, and heat exchanger network is complicated, and plant investment cost compare is high.
People is had to propose to adopt isothermal methanation reactor based on this feature, the relatively low temperature of reactor outlet one is controlled by by-product saturation steam, simultaneously at the adiabatic methanation reactor of follow-up series connection two-stage low temperature, the shortcoming of this flow process is can only by-product saturation steam, this steam quality is poor, cannot be used for the driving of turbine.
Summary of the invention
The purpose of this utility model is to solve the problems of the technologies described above, and provides that a kind of technique is simple, short flow, plant running and cost of investment are low, centralized recovery heat energy the single stage method coal synthetic natural gas system of by-product high-quality steam.
The system of single stage method coal synthetic natural gas technique, comprises the first absorption tower of the low temperature washing device for methanol connected successively, the shell side of the first feed gas heater or tube side, deep purifying devulcanizer, the tube side of the second feed gas heater or shell side, isothermal methanation reactor, the tube side of the first feed gas heater or shell side, the shell side of feedwater preheater or the second absorption tower of tube side, demineralized-water preheater, condensate separator and low temperature washing device for methanol; Wherein the shell side of the second feed gas heater or tube side outlet are also connected with the import of isothermal methanation reactor through the shell side of adiabatic methanator, vapor superheater or tube side successively; The outlet of described isothermal methanation reactor is also connected with the import of adiabatic methanation reactor through the tube side of the second feed gas heater or shell side, recycle gas compressor successively.
The tube side of described feedwater preheater or shell side also successively through the drum of isothermal methanation reactor, the tube side of vapor superheater or shell side respectively with the shell side of the second feed gas heater or tube side exports and multi-purpose station pipeline is connected.
First absorption tower of described low temperature washing device for methanol and second absorption tower share same Mathanol regenerating system.
Described isothermal methanation reactor and adiabatic methanation reactor all have upper and lower two catalyst activity beds, and the active bed of overlying catalyst is filled with for regulating CO and H
2comparison catalysts, the active bed of lower catalyst agent is filled with for catalysis CO and CO
2with H
2the catalyzer of methanation reaction.
Use the single stage method coal synthetic natural gas technique of said system, normal temperature raw gas removes H through the first absorption tower of low temperature washing device for methanol
2the impurity such as S are purified gas, described purified gas enters deep purifying devulcanizer and removes the impurity such as sulphur after preheating, then two strands are divided into after further preheating, first strand of purified gas enters adiabatic methanation reactor and carries out methanation reaction, the reaction gas going out adiabatic methanation reactor is together sent into isothermal methanation reactor with second strand of purified gas and is carried out methanation reaction after vapor superheater cooling, the reaction gas going out isothermal methanation reactor is divided into two strands, pressurize through recycle gas compressor after first burst of reaction gas cooling, adiabatic methanation reactor is together sent into again with first strand of purified gas, the second absorption tower sending into low temperature washing device for methanol after isolating phlegma by condensate separator again after second burst of reaction gas cooling removes CO
2and namely moisture obtain synthetic natural gas, described isothermal methanation reactor and adiabatic methanation reactor all have upper and lower two catalyst activity beds, and the active bed of overlying catalyst is filled with for regulating CO and H
2comparison catalysts, the active bed of lower catalyst agent is filled with for catalysis CO and CO
2with H
2the catalyzer of methanation reaction,
Hot steam is pressed through to regulate CO and the H in adiabatic methanation reactor and isothermal methanation reactor in the reacted reaction gas of the active bed of overlying catalyst in adding in the purified gas after preheating
2molar ratio be 1:2.95-3.05.
The tolerance of described first strand of purified gas accounts for the 20%-40% of described purified gas total amount, and the tolerance of described second strand of purified gas accounts for the 60%-80% of described purified gas total amount.
Regulate the tolerance of first strand of reaction gas to control the gas temperature of adiabatic methanation reactor outlet for 540-620 DEG C.
Feedwater first heats up through feedwater preheater and second strand of reaction gas indirect heat exchange, the drum sending into described isothermal methanation reactor again generates saturated middle pressure steam further, after pressing through hot steam in generating finally by vapor superheater and the reaction gas indirect heat exchange going out adiabatic reactor, the moisture be used for required for postreaction stove upper strata transformationreation part in purified gas after part adds described preheating, regulates CO and the H in the reacted reaction gas of the active bed of overlying catalyst in adiabatic methanation reactor and isothermal methanation reactor
2molar ratio, rest part is outer defeated.
First absorption tower of described low temperature washing device for methanol and second absorption tower share same Mathanol regenerating system.
Described isothermal methanation reactor and adiabatic methanation reactor all have upper and lower two catalyst activity beds, and the active bed of overlying catalyst is filled with for regulating CO and H
2comparison catalysts, the active bed of lower catalyst agent is filled with for catalysis CO and CO
2with H
2the catalyzer of methanation reaction.
Described isothermal methanation reactor inlet temperatures is 280-320 DEG C, and temperature out is 310-350 DEG C; The inlet temperature of adiabatic methanation reactor is 280 DEG C-320 DEG C.
Enter deep purifying devulcanizer after described purified gas and described second burst of reaction gas heat exchange heat up and remove the impurity such as sulphur; Go out after the purified gas of deep purifying devulcanizer and first burst of reaction gas heat exchange heat up and be divided into two strands.
The technique of contriver to existing raw gas synthetic natural gas is furtherd investigate, and makes following improvement: (1) is creationary eliminates traditional transformationreation device, and raw gas directly enters the first absorption tower of washing device for methanol, removes H
2the impurity such as S are purified gas, transformationreation and methanation reaction are combined in same reactor (isothermal methanation reactor and adiabatic methanation reactor) simultaneously and carry out, adopt one-step synthesis method reaction gas, effectively can shorten flow process, reduce relevant device, reduce facility investment and running cost; (2) owing to eliminating shift-reaction step, therefore raw gas cannot effectively decarburization in the first absorption tower, therefore in the end a step arranges the second absorption tower of washing device for methanol, play the effect of decarburization on the one hand, the moisture removed in reaction gas can also be washed simultaneously, directly obtain qualified dry natural gas, thus cancel the natural gas drying device of traditional coal synthetic natural gas flow process.(3) on the one hand, need in purified gas, to add steam to regulate CO and the H in adiabatic methanation reactor and isothermal methanation reactor in the reacted reaction gas of the active bed of overlying catalyst before methanation reaction
2ratio, on the other hand, because methanation reaction can generate water, the economic benefit removing recovery after this part water for cooling is limited, therefore contriver creationary the reaction gas going out adiabatic methanation reactor is mixed to send in isothermal methanation reactor with second strand of purified gas react, a part for the reaction gas gone out in isothermal methanation reactor is sent after circulation gas pressurization after purifying with first strand simultaneously and mix and send into adiabatic reactor, this just means that the water in reaction gas also enters in corresponding isothermal or adiabatic methanation reactor thereupon, high temperature after methanation reaction can make the water in gas exist in the form of water vapour, therefore the quantity of steam introduced by the external world can be greatly reduced, the water overwhelming majority produced in methanation reaction process is by system self reuse, the heat energy of system and water are fully recycled, there is the excellent effect of energy-conserving and environment-protective, (4) reaction gas going out adiabatic methanation reactor is mixed to send in isothermal methanation reactor with second strand of purified gas react, a part for the reaction gas gone out in isothermal methanation reactor is sent after circulation gas pressurization after purifying with first strand simultaneously and mix and send into adiabatic reactor, reacted portion gas circulation loopback is utilized to participate in methanation reaction again, the gas temperature controlling reactor outlet can be had, avoid reaction temperature out too high, improve the transformation efficiency of CO, guarantee the CH in synthetic gas
4concentration is up to standard, reduces selection and through engineering approaches difficulty that high temperature brings simultaneously, (5) contriver has taken into full account the problem that centralized heat energy reclaims, raw gas is utilized to need to heat up before methanation reaction, the technological process of lowering the temperature is needed after methanation reaction, purified gas before utilizing the first feed gas heater to make penetration depth purification reactor heats up through the first feed gas heater and described second strand of reaction gas indirect heat exchange, utilize the second feed gas heater to use the purified gas of deep purifying reactor and first strand of reaction gas indirect heat exchange heats up, thus rationally reclaim heat energy in system, further, hot steam is pressed through in order to obtain in high-quality, feedwater sends into the drum of isothermal methanation reactor after heating up through boiler water preheater and second strand of reaction gas indirect heat exchange, utilize the energy recovery that drum will discharge in isothermal methanation reactor, obtain saturated middle pressure steam, then it is overheated to be carried out above-mentioned saturated middle pressure steam by vapor superheater by the pyroreaction gas going out adiabatic reactor, obtain in high-quality and press through hot steam, pressing through steam in this part can part sent back system as required, rest part is outer defeated, can be used for the driving of steam turbine completely.On the other hand, because the pyroreaction gas that goes out adiabatic reactor carries out overheated to saturated middle pressure steam, temperature declines, and therefore can reduce high-temperature methanation equipment and relevant pipeline, reduce costs, and reduces the various problems that high temperature brings.(6) in order to realize conversion and methanation single step reaction, all arrange upper and lower two catalyst activity beds in isothermal methanation reactor and adiabatic methanation reactor, the active bed of overlying catalyst is filled with for regulating CO and H
2comparison catalysts, as Fe-Cr series, copper zinc system or cobalt-molybdenum series catalyst; The active bed of lower catalyst agent is filled with for catalysis CO and CO
2with H
2the catalyzer of methanation reaction; As nickel-base catalyst.When gas passes into, be introduced into the active bed of overlying catalyst and carry out CO transformationreation, then enter the active bed of lower catalyst agent and carry out methanation reaction, because two reactions are thermopositive reaction, thus also can realize the centralized recovery of heat energy.
Fully effectively overheated in order to what realize saturated middle pressure steam, guarantee the through engineering approaches of corresponding high temperature service and pipeline simultaneously and reduce investment, the gas temperature of adiabatic methanation reactor outlet preferably controls at 540-620 DEG C, and the control of this temperature is relevant with the tolerance of the first strand of reaction gas introducing adiabatic methanation reactor, those skilled in the art can require according to the gas temperature of adiabatic methanation reactor outlet the tolerance regulating the first strand of reaction gas introducing adiabatic methanation reactor.
For ensureing the steady running of system, generate qualified Sweet natural gas, preferred described isothermal methanation reactor inlet temperatures is 280-320 DEG C, and temperature out is 310-350 DEG C; The inlet temperature of adiabatic methanation reactor is 280 DEG C-320 DEG C.
Beneficial effect:
1. the utility model be based on gasification produce be rich in CO and H
2raw gas synthetic natural gas provide a kind of new scheme, technical process is simple and reliable, and heat recovery rate is high, and facility investment is low, and the Sweet natural gas produced meets the calorific value requirement of national standard (GB17820-2012) completely;
2. the technique adopting isothermal methanation reactor to combine with adiabatic methanation reactor, effectively reduces the quantity of high temperature service, reduces the manufacture of the materials such as equipment, pipeline, instrument valve and design difficulty and plant investment;
3. the CO conversion in traditional coal preparing natural gas flow process and methanation are synchronously carried out, shorten flow process, reduce investment and the occupation of land of device, the heat release of full factory is concentrated in together simultaneously, improve heat utilization efficiency, decrease tow taste heat;
4. adopt and supplement the mode of steam and to regulate in adiabatic methanation reactor and isothermal methanation reactor CO and H in the reacted reaction gas of the active bed of overlying catalyst
2ratio, reduce the possibility of carbon distribution in reactor, improve the operation stability of device; On the other hand, CO transformationreation needs to consume water, and methanation reaction can generate water, and the water that methanation reaction generates can be directly used in CO transformationreation, decreases the consumption of steam, simplifies heat recovery system.
5. adopt isothermal methanation reactor outlet synthetic gas to be circulated to adiabatic methanation reactor inlet, control the temperature of adiabatic methanation reactor outlet, ensure normally carrying out of methanation reaction, reduce generating run cost, the heat required for middle pressure saturation steam of overheated drum by-product is provided simultaneously.
Accompanying drawing explanation
Fig. 1 is the utility model process flow sheet and system diagram.
Wherein: E01---the first feed gas heater, E02---the second feed gas heater, E03---vapor superheater, E04---feedwater preheater, E05---demineralized-water preheater, R01---deep purifying reactor, R02---isothermal methanation reactor, R03---adiabatic methanation reactor, S01---drum, S02---condensate separator, K01---recycle gas compressor; A1-first absorption tower, A2-second absorption tower, A3-Mathanol regenerating system.
Embodiment
Below in conjunction with accompanying drawing, explanation is further explained to the utility model system:
The tube side of the shell side of the first absorption tower A1 of low temperature washing device for methanol, the shell side of the first feed gas heater E01 or tube side, deep purifying devulcanizer R01, the second feed gas heater E02 or tube side, isothermal methanation reactor R02, the first feed gas heater E01 or shell side, the shell side of feedwater preheater E04 or the second absorption tower A2 of tube side, demineralized-water preheater E05, condensate separator S02 and low temperature washing device for methanol; Wherein the shell side of the second feed gas heater E02 or tube side outlet are also connected with the import of isothermal methanation reactor R02 through the shell side of adiabatic methanator R03, vapor superheater E03 or tube side successively; The outlet of described isothermal methanation reactor R02 is also connected with the import of adiabatic methanation reactor R03 through the tube side of the second feed gas heater E02 or shell side, recycle gas compressor K01 successively.The tube side of described feedwater preheater E04 or shell side also successively through the drum S01 of isothermal methanation reactor R02, the tube side of vapor superheater E03 or shell side respectively with the shell side of the second feed gas heater E02 or tube side exports and multi-purpose station pipeline is connected.First absorption tower A1 of described low temperature washing device for methanol and second absorption tower A2 shares same Mathanol regenerating system A3.Described isothermal methanation reactor R02 and adiabatic methanation reactor R03 all has upper and lower two catalyst activity beds, and the active bed of overlying catalyst is filled with for regulating CO and H
2comparison catalysts, as Fe-Cr series, copper zinc system or cobalt-molybdenum series catalyst, the active bed of lower catalyst agent is filled with for catalysis CO and CO
2with H
2the catalyzer of methanation reaction, as nickel-base catalyst.
Process implementing case:
Consist of from the normal temperature raw gas of upstream coal gasification apparatus through recovery of heat: H
2: 17.95%mol; CH
4: 30ppm; N
2: 0.8%mol; CO:52.47%mol; CO
2: 7.45%mol; H
2s:0.43%; COS:<0.01%mol; NH
3+ HCN:0.032%mol; Ar:0.06%mol; H
2o:20.8%mol.Temperature: 168 DEG C, pressure: 3.8MPag, flow: 680676Nm3/h.
Normal temperature raw gas takes off A1 except H through the first absorption tower of low temperature washing device for methanol
2the impurity such as S are purified gas, described purified gas enters deep purifying devulcanizer R01 and removes the impurity such as sulphur after changing heat exchange to 170 DEG C-230 DEG C between the shell side of the first feed preheater E01 and second strand of reaction gas of tube side, then through first burst of reaction gas heat exchange to 280 DEG C-320 DEG C of the shell side of the second feed preheater E02 and tube side, hot steam is pressed through in passing in the purified gas after preheating to regulate CO and the H in adiabatic methanation reactor and isothermal methanation reactor in the reacted reaction gas of the active bed of overlying catalyst
2molar ratio be 1:2.95-3.05, then two strands are divided into, wherein, enter adiabatic methanation reactor R03 after the first strand of purified gas accounting for purified gas total amount 20%-40% (percent by volume) mixes with first strand of reaction gas from isothermal methanation reactor R02 and carry out methanation reaction, the inlet temperature controlling adiabatic methanation reactor R03 is 280-320 DEG C, temperature out is 540-620 DEG C, the reaction gas going out adiabatic methanation reactor R03 is together sent into isothermal methanation reactor R02 through vapor superheater E03 carry out methanation reaction to being mixed with second strand of purified gas after overheated from the saturated middle pressure steam of drum S01, controlling isothermal methanation reactor R02 inlet temperature is 280-320 DEG C, temperature out is 310-350 DEG C, the reaction gas going out isothermal methanation reactor R02 is divided into two strands, first burst of reaction gas (regulating the tolerance of first strand of reaction gas to control the gas temperature of adiabatic methanation reactor outlet for 540-620 DEG C) is forced into 3.5MPaG through recycle gas compressor K01 after the second feed gas heater E02 is cooled to 265 DEG C-225 DEG C with the purified gas heat exchange going out deep purifying devulcanizer R01, adiabatic methanation reactor R03 is together sent into again with first strand of purified gas, second strand of reaction gas cools to 40 DEG C further by boiler water preheater E04, demineralized-water preheater E05 again after the first feed gas heater E01 is cooled to 185 DEG C-235 DEG C with the purified gas heat exchange going out the first absorption tower A1, and the reaction gas after cooling is isolated through condensate separator S02 the second absorption tower sending into low temperature washing device for methanol after phlegma and taken off A2 and remove CO
2and namely moisture obtain synthetic natural gas, feedwater first changes through feedwater preheater E04 and second burst of reaction gas indirect thermal and is warming up to 180 DEG C-220 DEG C, the drum S01 sending into described isothermal methanation reactor R02 again generates the saturated middle pressure steam of 4.0MPaG-5.2MPaG further, after being pressed through hot steam finally by vapor superheater E03 in the overheated generation of the conversion gas of the high temperature going out adiabatic methanation reactor R03 400 DEG C-450 DEG C, part adds in the purified gas of the first feed gas heater E02 outlet to regulate CO and the H in reactor in the reacted reaction gas of the active bed of overlying catalyst
2molar ratio, rest part is outer defeated through multi-purpose station pipeline, can be used for the driving of steam turbine.
First absorption tower A1 of described low temperature washing device for methanol and second absorption tower A2 shares same Mathanol regenerating system A3.
Synthetic natural gas after treatment consists of: H
2: 0.6%mol; CH
4: 95.1%mol; N
2: 1.5%mol; CO:0.8%; CO
2: 1.1%mol; H
2o:0.8%mol, temperature: 33 DEG C, pressure: 3.075MPag, flow: 124875Nm3/h.Indices meets the requirement of GB17820-2012 to Sweet natural gas.
Adopt the usage quantity pressing through hot steam in the utility model technique to reduce by 51%, and press through hot steam in by-product 502t/h, CO transformation efficiency is 99.7%, H
2transformation efficiency is 99%, effectively reduce process unit investment about 10%, running cost about 6%, environmentally friendly.
Claims (3)
1. a single stage method coal synthetic natural gas system, it is characterized in that, comprise the first absorption tower of the low temperature washing device for methanol connected successively, the shell side of the first feed gas heater or tube side, deep purifying devulcanizer, the tube side of the second feed gas heater or shell side, isothermal methanation reactor, the tube side of the first feed gas heater or shell side, the shell side of feedwater preheater or the second absorption tower of tube side, demineralized-water preheater, condensate separator and low temperature washing device for methanol; Wherein the shell side of the second feed gas heater or tube side outlet are also connected with the import of isothermal methanation reactor through the shell side of adiabatic methanator, vapor superheater or tube side successively; The outlet of described isothermal methanation reactor is also connected with the import of adiabatic methanation reactor through the tube side of the second feed gas heater or shell side, recycle gas compressor successively;
Described isothermal methanation reactor and adiabatic methanation reactor all have upper and lower two catalyst activity beds, and the active bed of overlying catalyst is filled with for regulating CO and H
2comparison catalysts, the active bed of lower catalyst agent is filled with for catalysis CO and CO
2with H
2the catalyzer of methanation reaction.
2. single stage method coal synthetic natural gas system as claimed in claim 1, it is characterized in that, the tube side of described feedwater preheater or shell side also export with the second feed gas heater shell side or tube side respectively through the drum of isothermal methanation reactor, the tube side of vapor superheater or shell side successively and multi-purpose station pipeline is connected.
3. single stage method coal synthetic natural gas system as claimed in claim 1, it is characterized in that, the first absorption tower of described low temperature washing device for methanol and second absorption tower share same Mathanol regenerating system.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104774663A (en) * | 2015-04-27 | 2015-07-15 | 中国五环工程有限公司 | Synthetic natural gas prepared from one-step process coal and system thereof |
| CN107916151A (en) * | 2017-12-30 | 2018-04-17 | 西安长庆科技工程有限责任公司 | A kind of dewatering system and method for natural gas |
-
2015
- 2015-04-27 CN CN201520257691.3U patent/CN204569865U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104774663A (en) * | 2015-04-27 | 2015-07-15 | 中国五环工程有限公司 | Synthetic natural gas prepared from one-step process coal and system thereof |
| CN107916151A (en) * | 2017-12-30 | 2018-04-17 | 西安长庆科技工程有限责任公司 | A kind of dewatering system and method for natural gas |
| CN107916151B (en) * | 2017-12-30 | 2023-10-20 | 西安长庆科技工程有限责任公司 | Dehydration system and method for natural gas |
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