CN103849442A - Method for preparing natural gas by utilizing synthesis gas - Google Patents
Method for preparing natural gas by utilizing synthesis gas Download PDFInfo
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- CN103849442A CN103849442A CN201210493613.4A CN201210493613A CN103849442A CN 103849442 A CN103849442 A CN 103849442A CN 201210493613 A CN201210493613 A CN 201210493613A CN 103849442 A CN103849442 A CN 103849442A
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Abstract
The invention discloses a method for preparing natural gas by utilizing synthesis gas. After the synthesis gas is subjected to desulfurization and decarbonization, the synthesis gas enters a three-stage adiabatic reactor and is subjected to a methanation reaction, carbon monoxide and carbon dioxide in the synthesis gas undergo a reaction with hydrogen gas to generate methane, and then through condensing separation, the natural gas containing more than 95% of methane is obtained. With adopting of the method to prepare the natural gas, not only can the natural gas with high methane content be prepared, but also the method has the advantages of simple process and lower energy consumption.
Description
Technical field
The present invention relates to utilize synthetic gas to prepare the method for Sweet natural gas, belong to the clean Efficient Conversion field of coal.
Background technology
Sweet natural gas is a kind of energy of high-efficiency cleaning.In recent years, along with " Shan gas is gone to the capital ", " in succession the building up and come into operation of the national combustion gas conveying engineering such as West-east Gas, the demand of Sweet natural gas is explosive growth.It is predicted, 2015, the demand of Natural Gas In China will reach 1,700 hundred million Nm
3~ 2,100 hundred million Nm
3, and the gas production of the same period can only reach 1,400 hundred million Nm
3, insufficiency of supply-demand approximately 30,000,000,000 Nm
3~ 700 hundred million Nm
3.In order to solve the imbalance between supply and demand problem of China's natural gas, also actively utilize the natural gas source of other countries of the world except the resource of basing on our country, also need to seek other alternative route.
The coal resources that utilize China relatively to enrich, producing Sweet natural gas by coal based synthetic gas is an effective way that solves Sweet natural gas imbalance between supply and demand." Zhejiang, new Guangdong ", " new Shandong " exclusive pipeline of coal preparing natural gas of Sinopec planning construction, gas transmission ability is 60,000,000,000 Nm
3/ a.Because insufficiency of supply-demand is huge, coal preparing natural gas project Cheng Liao China new bright spot of investment of coal chemical technology after coal liquefaction.At present domesticly reached 32 in the coal to SNG project of building and planned, planning production capacity reaches 1,168 hundred million Nm
3/ a.Wherein, existing 4 projects have obtained the official approval of National Development and Reform Committee and have started and built, and add up to production capacity 15,100,000,000 Nm
3/ a.Therefore, coal preparing natural gas has broad prospects.
Coal preparing natural gas is all generally first gasification to be produced to synthetic gas, and synthetic gas again methanation generates Sweet natural gas.The technology that gasification produces synthetic gas is comparatively ripe, and the key of coal preparing natural gas technology is the methanation of synthetic gas.Chinese patent 200910055548.5 discloses a kind of " utilizing synthetic gas to prepare the processing method of Sweet natural gas ", in this technique methane synthesis unit, synthetic gas is by 3～5 grades of methane building-up reactionss, the tail gas of every order reaction has part to loop back this stage reactor or front stage reactor, and reacted tail gas enters natural gas conditioning unit.
For another example Chinese patent 201110268668.0 discloses a kind of " methanation process of coal synthetic natural gas processed ", this technique is divided into three strands by coal generating gas through the synthetic gas of purification and decarburization, first strand of synthetic gas and circulation gas enter the first methanator after mixing, after mixing with second strand of synthetic gas, the gas of the first methanator outlet enters the second methanator, after mixing with the 3rd strand of synthetic gas, the gas of the second methanator outlet enters front three alkylation reactors, after separating a part of gas enter recycle compressor and boost after front three alkylation reactors being carried out gas cooling as circulation gas, remaining gas enters the 4th successively, the 5th or pregnancy alkylation reactors carry out methanation reaction, in the gas of last methanator outlet, methane contents on dry basis is greater than 95%.
Current domestic synthetic gas is produced Sweet natural gas, the band circulation technologies that adopt more, and circulation has brought the drawbacks such as investment is high, energy consumption is high.The present invention adopts and is not with circulation technology, and flow process is simple, reduced investment, and energy consumption is low.
Summary of the invention
The object of this invention is to provide a kind of method of utilizing synthetic gas to prepare Sweet natural gas.Utilize the method can make the Sweet natural gas that calorific value is higher, foreign matter content is low.
Synthetic gas, through after desulfurization and decarburization, is carried out to three grades of methanation reactions, and the hydrogen in synthetic gas and carbon monoxide and carbon dioxide reaction generate methane, dewater through condensation, can obtain containing more than 95% Sweet natural gas of methane.
Methanation reaction described above catalyzer used is the right cylinder of the aspect ratio take Ni in aluminum oxide and (or) on magnesium oxide as 1 preferably.
First step methanator described above is two strands of gas feeds preferably.First strand of gas is from reactor head charging, and the temperature in of gas is preferably 180-325 ℃; Second strand of gas is preferably from the 1/4-3/4 charging of height for reactor, and the temperature in of gas is preferably 180-325 ℃, and flow is preferably the 20%-60% of first burst of charging, and reactor pressure is preferably 1.0-4.5MPa.
The temperature in of second stage methanator gas described above is preferably 200-355 ℃, the low 0.04-0.17MPa of pressure of pressure ratio first step methanator.
The temperature in of third stage methanator gas described above is preferably 305-365 ℃, the low 0.04-0.17MPa of pressure of pressure ratio second stage methanator.
Synthetic gas described above is 18-22%(v/v through CO content after desulfurization and decarburization), H
2content is 65-70%(v/v), CH
4content is 8-10%(v/v).
The exit gas of first step methanator described above by an interchanger by the gas heating after desulfurization and decarburization, the cooling second stage methanator that enters again afterwards.
The inventive method is prepared Sweet natural gas not only can make the Sweet natural gas that methane content is high, and flow process is simple, and energy consumption is lower.
Accompanying drawing explanation
Fig. 1 is the block flowsheet schematic diagram of embodiment of the present invention method.
Embodiment
Below in conjunction with embodiment, the present invention is described in further detail.But this should be interpreted as to the scope of the above-mentioned theme of the present invention only limits to following embodiment.
Embodiment 1
It is as follows that the present embodiment utilizes synthetic gas to prepare the method for Sweet natural gas, and schematic flow sheet is shown in Fig. 1:
By synthetic gas, through desulfurization, decarburization, the gas mixture obtaining composition (vol%) is: H
268, CH
49, CO 19, CO
23, total sulfur content is less than 0.1ppm, under the nickel catalysis being carried on aluminum oxide, carries out methanation reaction.The pressure of first step methanator is about 4.5MPa, and reactor head feed entrance temperature is about 200 ℃; Introduce one charging in addition at 1/4 place that is height overall apart from reactor inlet, feed rate is 60% of first burst of charging, and feeding temperature is identical with first burst of charging with composition.
Gas from first step methanator out, by the gas heating after desulfurization and decarburization, be cooled to again afterwards 200 ℃ by interchanger, enter second stage methanator.After the methanator of the second stage, be cooled to 305 ℃, enter second stage methanator, exit gas obtains more than 95% Sweet natural gas of methane content through condensation separation.
4Nm
3synthetic gas can make Sweet natural gas 1Nm
3.
Embodiment 2
It is as follows that the present embodiment utilizes synthetic gas to prepare the method for Sweet natural gas, and schematic flow sheet is shown in Fig. 1:
By synthetic gas, through desulfurization, decarburization, the gas mixture obtaining composition (vol%) is: H
268, CH
49, CO 19, CO
23, total sulfur content is less than 0.1ppm, under the nickel catalysis being carried on aluminum oxide, magnesia mixture, carries out methanation reaction.The pressure of first step methanator is about 2.5MPa, and reactor head feed entrance temperature is about 280 ℃; Introduce one charging in addition at 1/2 place that is height overall apart from reactor inlet, feed rate is 40% of first burst of charging, and feeding temperature is identical with first burst of charging with composition.
Gas from first step methanator out, by the gas heating after desulfurization and decarburization, be cooled to again afterwards 320 ℃ by interchanger, enter second stage methanator.After the methanator of the second stage, be cooled to 345 ℃, enter second stage methanator, exit gas obtains more than 95% Sweet natural gas of methane content through condensation separation.
4.2Nm
3synthetic gas can make Sweet natural gas 1Nm
3.
Embodiment 3
It is as follows that the present embodiment utilizes synthetic gas to prepare the method for Sweet natural gas, and schematic flow sheet is shown in Fig. 1:
By synthetic gas, through desulfurization, decarburization, the gas mixture obtaining composition (vol%) is: H
268, CH
49, CO 19, CO
23, total sulfur content is less than 0.1ppm, under the nickel catalysis being carried on aluminum oxide, magnesia mixture, carries out methanation reaction.The pressure of first step methanator is about 1.0MPa, and reactor head feed entrance temperature is about 320 ℃; Introduce one charging in addition at 3/4 place that is height overall apart from reactor inlet, feed rate is 20% of first burst of charging, and feeding temperature is identical with first burst of charging with composition.
Gas from first step methanator out, by the gas heating after desulfurization and decarburization, be cooled to again afterwards 350 ℃ by interchanger, enter second stage methanator.After the methanator of the second stage, be cooled to 365 ℃, enter second stage methanator, exit gas obtains more than 95% Sweet natural gas of methane content through condensation separation.
4.3Nm
3synthetic gas can make Sweet natural gas 1Nm
3.
Claims (7)
1. a method of utilizing synthetic gas to prepare Sweet natural gas, by the hydrogen in synthetic gas and carbon monoxide and carbon dioxide reaction generation methane, it is characterized in that: after synthetic gas process desulfurization and decarburization, carry out methanation reaction through the reaction of high order that comprises three reactors, dewater through condensation, obtain containing more than 95% Sweet natural gas of methane.
2. method according to claim 1, is characterized in that: described first step methanator has two strands of gas feeds, and first strand of gas is from reactor head charging, and the temperature in of gas is 180-325 ℃; Second strand of gas is from the 1/4-3/4 charging of height for reactor, and the temperature in of gas is 180-325 ℃, and flow is the 20%-60% of first burst of charging, and reactor pressure is 1.0-4.5MPa.
3. method according to claim 1, is characterized in that: the temperature in of described second stage methanator gas is 200-355 ℃, the low 0.04-0.17MPa of pressure of pressure ratio first step methanator.
4. method according to claim 1, is characterized in that: the temperature in of described third stage methanator gas is 305-365 ℃, the low 0.04-0.17MPa of pressure of pressure ratio second stage methanator.
5. method according to claim 1, is characterized in that: synthetic gas is 18-22%(v/v through CO content after desulfurization and decarburization), H
2content is 65-70%(v/v), CH
4content is 8-10%(v/v).
6. method according to claim 1, is characterized in that: the exit gas of first step methanator by an interchanger by the gas heating after desulfurization and decarburization, the cooling second stage methanator that enters again afterwards.
7. according to the method described in claim 1-6 any one claim, it is characterized in that: the catalyzer of methanation reaction is aspect ratio take Ni in aluminum oxide and/or on magnesium oxide is 1 right cylinder.
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| CN201210493613.4A CN103849442A (en) | 2012-11-28 | 2012-11-28 | Method for preparing natural gas by utilizing synthesis gas |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104152198A (en) * | 2014-07-21 | 2014-11-19 | 中国五环工程有限公司 | Methanation reaction process |
| CN105062593A (en) * | 2015-08-18 | 2015-11-18 | 中国神华能源股份有限公司 | Methane preparation technological system |
| CN105861085A (en) * | 2015-01-23 | 2016-08-17 | 中国石化工程建设有限公司 | Preparation method of natural gas substitute from synthetic gas |
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| US4205961A (en) * | 1977-07-02 | 1980-06-03 | Metallgesellschaft | Process of producing a natural gas substitute |
| CN101705128A (en) * | 2009-07-14 | 2010-05-12 | 上海国际化建工程咨询公司 | Adiabatic methanation process and device for preparing synthetic natural gas |
| CN101812339A (en) * | 2010-04-15 | 2010-08-25 | 大唐国际化工技术研究院有限公司 | Method and device for producing synthetic natural gas, and natural gas product thereof |
| CN101985574A (en) * | 2009-07-29 | 2011-03-16 | 华东理工大学 | Process for preparing natural gas from synthetic gas |
| CN102660339A (en) * | 2012-04-27 | 2012-09-12 | 阳光凯迪新能源集团有限公司 | Gas-steam efficient cogeneration process and system based on biomass gasification and methanation |
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2012
- 2012-11-28 CN CN201210493613.4A patent/CN103849442A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4205961A (en) * | 1977-07-02 | 1980-06-03 | Metallgesellschaft | Process of producing a natural gas substitute |
| CN101705128A (en) * | 2009-07-14 | 2010-05-12 | 上海国际化建工程咨询公司 | Adiabatic methanation process and device for preparing synthetic natural gas |
| CN101985574A (en) * | 2009-07-29 | 2011-03-16 | 华东理工大学 | Process for preparing natural gas from synthetic gas |
| CN101812339A (en) * | 2010-04-15 | 2010-08-25 | 大唐国际化工技术研究院有限公司 | Method and device for producing synthetic natural gas, and natural gas product thereof |
| CN102660339A (en) * | 2012-04-27 | 2012-09-12 | 阳光凯迪新能源集团有限公司 | Gas-steam efficient cogeneration process and system based on biomass gasification and methanation |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104152198A (en) * | 2014-07-21 | 2014-11-19 | 中国五环工程有限公司 | Methanation reaction process |
| CN105861085A (en) * | 2015-01-23 | 2016-08-17 | 中国石化工程建设有限公司 | Preparation method of natural gas substitute from synthetic gas |
| CN105861085B (en) * | 2015-01-23 | 2019-05-17 | 中国石化工程建设有限公司 | A kind of method of synthesis gas system substitution natural gas |
| CN105062593A (en) * | 2015-08-18 | 2015-11-18 | 中国神华能源股份有限公司 | Methane preparation technological system |
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Application publication date: 20140611 |