CN102827657A - Isothermal methanation process method for coal to substitute natural gas - Google Patents
Isothermal methanation process method for coal to substitute natural gas Download PDFInfo
- Publication number
- CN102827657A CN102827657A CN2012103082288A CN201210308228A CN102827657A CN 102827657 A CN102827657 A CN 102827657A CN 2012103082288 A CN2012103082288 A CN 2012103082288A CN 201210308228 A CN201210308228 A CN 201210308228A CN 102827657 A CN102827657 A CN 102827657A
- Authority
- CN
- China
- Prior art keywords
- methanation
- gas
- isothermal
- natural gas
- process method
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Images
Landscapes
- Industrial Gases (AREA)
Abstract
The invention discloses an isothermal methanation process method for coal to substitute natural gas. Specifically, upstream purified synthetic gas enters one or more methanation reactors after fine desulfurization for undergoing a methanation reaction, and two-stage methanation is adopted in the methanation reactor(s). At a first stage, methanation is performed in one or more isothermal methanation reactors; and at a second stage, methanation is performed in a heat-insulated methanation reactor. The isothermal methanation process method has the advantages of saving in energy, environment friendliness, small investment and easiness in localization.
Description
Technical field
The invention belongs to coal preparing natural gas applied technical field, be specifically related to a kind of isothermal methanation process method of coal preparing natural gas.
Background technology
The characteristics of China's endowment of resources are " rich coal, oil starvation, weak breaths ".The ring Bohai Sea, the Yangtze River Delta, Pearl River Delta three large economy bands are huge to Natural Gas Demand, and ground rich coal resources such as the Inner Mongol, Xinjiang, but transportation cost is high.Therefore, the geographic coal resources of rich coal are changed into Sweet natural gas on the spot, the another grand strategy that becomes after coal generating, coal system oil, coal system alkene is selected.
In recent years, along with increasing substantially of the flourish of Coal Chemical Industry industry and natural gas consumption amount, China's coal preparing natural gas industry obtains tremendous development, becomes the coal chemical technology bright spot of investment.The large amounts of gas maked coal project of a collection of investment in 2009 starts successively, and China coal preparing natural gas field presents the good momentum of development.Since 2010, along with the inlet natural gas price increase, China coal preparing natural gas market is persistently overheating.
In the long run, the trend that the China's natural gas price progressively goes up confirms that therefore, the cost advantage of coal preparing natural gas will manifest gradually, and economic benefit is very considerable, and CHINESE COAL preparing natural gas industry development has a extensive future.
Develop coal preparing natural gas technology and then have good economic benefit in the current soaring oil prices epoch at the big moulded coal preparing natural gas of coal district construction device; To solving the problem of complex utilization of coal resources in China; Alleviate the present situation of China's hydrocarbon resources shortage; Safeguard the energy security of China, realize energy-saving and emission-reduction, protect environment significant.
The coal gas staple that gasification produces is CO, CO
2, H
2, H
2O, this coal gas is low because of calorific value, and CO is toxic, before 10 years, is progressively replaced by Sweet natural gas; Discover, under catalyst action, can CO in the coal gas all be converted into methane, Here it is Sweet natural gas.The process that CO is converted into methane promptly is the methanation reaction process, and following reaction takes place its process:
CO?+?3H
2?←→?CH
4?+?H
2O +206.16kJ/mol (1)
CO
2?+?4H
2?←→?CH
4?+?2H
2O +165.08kJ/mol (2)
CO?+?H
2O?←→?CO
2?+?H
2 +41.19kJ/mol ?(3)
Above-mentioned reaction (1), (2) are methanation reaction, and two reactions are strong exothermal reaction, and accelerated reaction under the high temperature helps the methane reaction balance and moves right under the low temperature, be in 280-420 ℃ in temperature of reaction, and the equilibrium constant is very big; Reaction (2) is the carbon monodixe conversion reaction, is a reversible balanced reaction.
In ammonia synthesizing industry, methanation reaction is used for removing a small amount of CO of decarbonization gas and CO as a kind of purification techniques
2, reach the purpose made from extra care synthetic gas, with the protection ammonia synthesis catalyst.In this uses, owing to CO and CO in the synthetic gas
2Content extremely low (CO:0.35-0.6%, CO
2: 0.05%); Methanator adopts the heat-insulating fixed-bed reactor usually; Reaction temperature rising overheating problem can not occur, sometimes generally at 31.7-50 ℃; CO is lower than 0.35% in the synthetic gas as crossing, and can not keep autothermal equilibrium (flow setting is the synthetic gas that methanator outlet hot gas is used for heats cold) on the contrary.
CO content higher (generally at 5-25% (V)) in the synthetic gas of coal preparing natural gas, and the thermal discharge of methanation reaction is very big, at above-mentioned synthetic gas (H
2: CO=3:1), the CO of revolutionization 1% and CO
2Thermal insulation warming be respectively 72.59 ℃ and 57.12 ℃.The temperature in of methanator receives the restriction of nickle carbonoxide formation and light-off temperature, and in order to obtain high methanation transformation efficiency, temperature in is about 280 ℃.When the reaction mixture gas body passed through the adiabatic beds, temperature sharply raise, and too high temperature can cause catalyst deactivation on the one hand, is unfavorable for providing reactor outlet CH on the other hand
4Content.
The methanation of current industrialized coal preparing natural gas all is to adopt a plurality of adiabatic methanation reactors in series, and methanation reaction is carried out in classification, and particularly main methanator is the high-temperature heat insulation methanator.Major technology has: strange (Lurgi) company in German Shandong, Denmark Top rope (Tops φ e) company's T REMPTM technology, the GRG of Britain Davy company technology.
The seventies in 20th century, LURGI, Sasol begin to carry out the research and the test of gas methanation production synthetic natural gas, and through the experiment of two and half industrial test factories, confirmation can be produced qualified synthetic natural gas.The transformation efficiency of methanation reaction CO can reach 100%, CO
2Transformation efficiency can reach 95%, and low heat value is 35.581MJ/Nm
3Simultaneously, on the llanura of North Dakota, built llanura synthol factory (GPSP), adopting lignite resource abundant on the llanura is the raw material production synthetic natural gas.This factory brought into operation in 1984, and this factory is so far still in normal operation.
Rope company of Top exploitation methanation technology can trace back to the later stage seventies 20th century, the methanation circulation technology (TREMP of the said firm's exploitation
TM) technology has abundant operating experience and substantive process certification, guaranteed that this technology can be used in commercialization.
In the twentieth century latter stage nineties, Britain Davy company has obtained the GRG technology is externally transferred the possession of the exclusive right of permission, and has further developed GRG technology and catalyzer, and has passed through the industriallization checking.
Ac.cn is also making big quantity research aspect the coal preparing natural gas, main experience also is the research and development that concentrates on the high-temperature methanation catalyst performance.
The common problem of above-mentioned process method is:
(1) adopt a plurality of adiabatic methanation reactors in series, main methanator adopts resistant to elevated temperatures methanation catalyst, and service temperature is about 650 ℃.
(2) in order not make main methanator not produce overtemperature, need to adopt gas circulation, recycle ratio generally about 0.75, increases energy consumption.
(3) because service temperature about 650 ℃, has proposed requirements at the higher level to equipment, pipeline, valve design, cause plant investment to increase, production cost also increases thereupon.
Summary of the invention
The objective of the invention is to provides a kind of high-temperature operation and methanation overtemperature risk that can solve the high concentration CO methanation, the isothermal methanation process method that is used for the high concentration CO methanation that can prolong the work-ing life of methanation catalyst again to the above-mentioned deficiency that prior art exists.
The technique means scheme that the present invention adopts is following:
A kind of isothermal methanation process method of coal preparing natural gas is characterized in that it specifically comprises the steps:
To be fed into from the synthetic gas that the upper reaches purified feed gas heater with from after the heat exchange of adiabatic methanation reactor outlet hot gas; Be preheated to 280-300 ℃; Gas after the preheating gets into smart desulfurizer, total sulfur in the synthetic gas is controlled at below the 30ppb, with the protection methanation catalyst; Synthetic gas gets into one or more isothermal methanation reactor drums and carries out methanation reaction subsequently; The hot gas that goes out the isothermal methanation reactor drum gets into the MP steam of vapor superheater superheater by-product, gets into waste heat boiler subsequently, by-product 4.0MPa MP steam; Get into the adiabatic methanation reactor drum after its temperature reduced to 280-300 ℃; Further unreacted CO is changed into methane, make that CO content is lower than 5-10ppm in the exit gas, reacted gas is through former glassware preheater, feedwater preheater, water cooler cooling; Get into and directly to obtain containing methane 94-98%, high heating value 37.38-38.37MJ/Nm after gas-liquid separator is told water of condensation
3Synthetic natural gas.
H in the described synthetic gas
2+ CO
2And CO+CO
2Mol ratio be 3.0-6.5:1, CO
2Content is 0.5-3.5%, and CO content is 5-25%, and total sulfur is less than 0.1ppm.
Described isothermal methanation reactor drum is vertical fixed tube sheet heat exchanger; Be equipped with in the pipe homemade in warm methanation catalyst; Adopting boiling water to remove reaction heat controlling reactor temperature between pipe is 380-420 ℃; The reactor outlet temperature is 350-420 ℃, and the hot(test)-spot temperature in the isothermal methanation reactor tube is no more than 420 ℃.
The system pressure of described methanation reaction is controlled between the 2.5-6.5MPa.
The steam water interface on the shell side top of described isothermal methanation reactor drum gets into the steam pockets at its top; Separate the back and produce the 10MPa HP steam; Boiling water in the drum loops back the shell side bottom of reactor drum again according to gravity; Constitute a gravity circulation loop, constantly remove methanation reaction heat, keep the temperature of reaction of isothermal methanation.
Described isothermal methanation process method also is applicable to the coke-oven gas synthetic natural gas after the purification.
The present invention has following advantage:
(1) the present invention adopts circulating boiling water to remove the reaction heat of methanation, and the reactor catalyst bed is carried out under the temperature of gentleness, can use homemade in warm methanation catalyst, prolong catalyzer work-ing life greatly.Reduced running cost, industrial significance and remarkable in economical benefits;
(2) the present invention need not adopt gas circulation, reduces energy consumption;
(3) the present invention only need adopt an isothermal methanation reactor drum and an adiabatic methanation reactor drum just can make that CO content is less than 10ppm in the final synthetic natural gas;
(4) the present invention has reduced the maximum operating temperature of methanation device, has reduced the requirement to equipment, pipeline, valve material;
(5) the present invention can simplify the technical process of existing coal preparing natural gas device, economizer construction.
Description of drawings
Fig. 1 is the process flow diagram of embodiment of the invention coal preparing natural gas, and wherein major equipment comprises: 1, feed gas heater; 2, smart desulfurizer; 3, isothermal methanation reactor drum; 4, vapor superheater; 5, waste heat boiler; 6, adiabatic methanation reactor drum; 7, feedwater preheater; 8, water cooler; 9, gas-liquid separator; 10, steam pockets.
Embodiment
Below in conjunction with accompanying drawing and embodiment the present invention is elaborated.
Embodiment
Shown in accompanying drawing 1, the method for the embodiment of the invention is mainly accomplished through following system, and this system mainly comprises: (a) smart desulfurizer of controlling total sulfur content in the reactor feed gas; (b) feed gas heater of carrying out preheating for reactor feed gas; (c) isothermal methanation reactor drum as main reactor; (d) one is used for HP steam superheated vapor superheater and for the useless pot of the MP steam of controlling the second methanator gasinlet temperature; (e) adiabatic methanation reactor drum that is used for controlling product Sweet natural gas CO content.
The isothermal methanation process method of coal preparing natural gas is carried out as follows:
To be fed into from the synthetic gas that the upper reaches purified feed gas heater with from after the heat exchange of adiabatic methanation reactor outlet hot gas; Be preheated to 280 ℃; Gas after the preheating gets into smart desulfurizer, total sulfur in the synthetic gas is controlled at below the 30ppb, with the protection methanation catalyst; Synthetic gas gets into one or more isothermal methanation reactor drums and carries out methanation reaction subsequently; The hot gas that goes out the isothermal methanation reactor drum gets into the MP steam of vapor superheater superheater by-product, gets into waste heat boiler subsequently, by-product 4.0MPa MP steam; Get into the adiabatic methanation reactor drum after its temperature reduced to 280 ℃; Further unreacted CO is changed into methane, make that CO content is lower than 5ppm in the exit gas, reacted gas is through former glassware preheater, feedwater preheater, water cooler cooling; Get into and directly to obtain containing methane 96%, high heating value 37.87 MJ/Nm after gas-liquid separator is told water of condensation
3Synthetic natural gas.
H in the described synthetic gas
2+ CO
2And CO+CO
2Mol ratio be 5:1, CO
2Content is 2%, and CO content is 15%, and total sulfur is less than 0.1ppm.
Described isothermal methanation reactor drum is vertical fixed tube sheet heat exchanger; Be equipped with in the pipe homemade in warm methanation catalyst; Adopting boiling water to remove reaction heat controlling reactor temperature between pipe is 400 ℃; The reactor outlet temperature is 350 ℃, and the hot(test)-spot temperature in the isothermal methanation reactor tube is no more than 420 ℃.
The system pressure of described methanation reaction is controlled at 3.5MPa.
The steam water interface on the shell side top of described isothermal methanation reactor drum gets into the steam pockets at its top; Separate the back and produce the 10MPa HP steam; Boiling water in the drum loops back the shell side bottom of reactor drum again according to gravity; Constitute a gravity circulation loop, constantly remove methanation reaction heat, keep the temperature of reaction of isothermal methanation.
Claims (6)
1. the isothermal methanation process method of a coal preparing natural gas is characterized in that it specifically comprises the steps:
In the methanation synthesis technique; To be fed into from the synthetic gas that the upper reaches purified feed gas heater with from after the heat exchange of adiabatic methanation reactor outlet hot gas; Be preheated to 280-300 ℃; Gas after the preheating gets into smart desulfurizer, total sulfur in the synthetic gas is controlled at below the 30ppb, with the protection methanation catalyst; Synthetic gas gets into one or more isothermal methanation reactor drums and carries out methanation reaction subsequently; The hot gas that goes out the isothermal methanation reactor drum gets into the MP steam of vapor superheater superheater by-product, gets into waste heat boiler subsequently, by-product 4.0MPa MP steam; Get into the adiabatic methanation reactor drum after its temperature reduced to 280-300 ℃; Further unreacted CO is changed into methane, make that CO content is lower than 5-10ppm in the exit gas, reacted gas is through former glassware preheater, feedwater preheater, water cooler cooling; Get into and directly to obtain containing methane 94-98%, high heating value 37.38-38.37MJ/Nm after gas-liquid separator is told water of condensation
3Synthetic natural gas.
2. according to the isothermal methanation process method of claims 1 described coal preparing natural gas, it is characterized in that H in the described synthetic gas
2+ CO
2And CO+CO
2Mol ratio be 3.0-6.5:1, CO
2Content is 0.5-3.5%, and CO content is 5-25%, and total sulfur is less than 0.1ppm.
3. according to the isothermal methanation process method of claims 1 described coal preparing natural gas; It is characterized in that; Described isothermal methanation reactor drum is vertical fixed tube sheet heat exchanger, be equipped with in the pipe homemade in warm methanation catalyst, adopting boiling water to remove reaction heat controlling reactor temperature between pipe is 380-420 ℃; The reactor outlet temperature is 350-420 ℃, and the hot(test)-spot temperature in the isothermal methanation reactor tube is no more than 420 ℃.
4. according to the isothermal methanation process method of claims 1 described coal preparing natural gas, it is characterized in that the system pressure of described methanation reaction is controlled between the 2.5-6.5MPa.
5. according to the isothermal methanation process method of claims 1 described coal preparing natural gas; It is characterized in that the steam water interface on the shell side top of described isothermal methanation reactor drum gets into the steam pockets at its top, separate the back and produce the 10MPa HP steam; Boiling water in the drum loops back the shell side bottom of reactor drum again according to gravity; Constitute a gravity circulation loop, constantly remove methanation reaction heat, keep the temperature of reaction of isothermal methanation.
6. according to the isothermal methanation process method of claims 1 described coal preparing natural gas, it is characterized in that described isothermal methanation process method also is applicable to the coke-oven gas synthetic natural gas after the purification.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012103082288A CN102827657A (en) | 2012-08-27 | 2012-08-27 | Isothermal methanation process method for coal to substitute natural gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012103082288A CN102827657A (en) | 2012-08-27 | 2012-08-27 | Isothermal methanation process method for coal to substitute natural gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN102827657A true CN102827657A (en) | 2012-12-19 |
Family
ID=47330971
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2012103082288A Pending CN102827657A (en) | 2012-08-27 | 2012-08-27 | Isothermal methanation process method for coal to substitute natural gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102827657A (en) |
Cited By (16)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103343025A (en) * | 2013-06-08 | 2013-10-09 | 东华工程科技股份有限公司 | Process for synthesizing natural gas employing methanation of calcium carbide furnace gas |
| CN103695058A (en) * | 2013-12-19 | 2014-04-02 | 中国海洋石油总公司 | Novel methanation reaction process for preparing synthetic natural gas |
| CN104164264A (en) * | 2014-08-19 | 2014-11-26 | 赛鼎工程有限公司 | Process for preparing substitute liquefied natural gas (LNG) with coke-oven gas |
| CN104357117A (en) * | 2014-10-31 | 2015-02-18 | 西南化工研究设计院有限公司 | Non-circulating methanation process of coal-based synthetic natural gas and liquefied natural gas |
| CN104845689A (en) * | 2014-02-18 | 2015-08-19 | 中国石油化工股份有限公司 | Technology for preparing synthetic natural gas through methanation of coal-based synthetic gas |
| CN105087091A (en) * | 2014-05-08 | 2015-11-25 | 中国石油化工股份有限公司 | Technology for preparing synthetic natural gas |
| CN106794438A (en) * | 2014-10-15 | 2017-05-31 | 托普索公司 | It is used for the containment system of the device of catalyst protection with the safety interlock tripping operation in reactor or down periods |
| CN107090320A (en) * | 2017-06-16 | 2017-08-25 | 中国石油大学(华东) | Based on the synthesis gas fluid bed preparing natural gas by methanation device being dehydrated between level |
| CN107868686A (en) * | 2017-11-15 | 2018-04-03 | 太原理工大学 | A kind of energy-saving method without circulation coal synthetic natural gas full methanation |
| CN107922862A (en) * | 2015-07-16 | 2018-04-17 | 前苏伊士环能集团 | The apparatus and method for generating synthesis gas |
| CN108219879A (en) * | 2016-12-14 | 2018-06-29 | 中国石化工程建设有限公司 | Coal system substitute natural gas without cycle methanation in presence of sulfur technique |
| CN109266413A (en) * | 2018-10-30 | 2019-01-25 | 青岛联信催化材料有限公司 | A method of synthetic natural gas is produced using hydrogen retrieval impermeable gas |
| CN109593581A (en) * | 2018-12-21 | 2019-04-09 | 惠生工程（中国）有限公司 | It is a kind of once to pass through methanation process |
| CN109609221A (en) * | 2018-12-21 | 2019-04-12 | 惠生工程（中国）有限公司 | A kind of semi-coke furnace tail gas fine de-sulfur and isothermal methanation process |
| CN110903870A (en) * | 2018-09-18 | 2020-03-24 | 中国石油化工股份有限公司 | Process for preparing methane by single pass of coal-based synthesis gas in slurry bed |
| CN111511882A (en) * | 2017-11-30 | 2020-08-07 | 浦项产业科学硏究院 | Preparation method and preparation device of high-calorific-value synthetic natural gas |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101649233A (en) * | 2009-07-14 | 2010-02-17 | 上海国际化建工程咨询公司 | Isothermal methanation process and device for the preparation of synthetic natural gas |
| 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 |
| CN101775319A (en) * | 2010-02-11 | 2010-07-14 | 山西科灵环境工程设计技术有限公司 | Method for producing synthetic natural gas SNG from coal and processing installation thereof |
| CN101880559A (en) * | 2010-06-18 | 2010-11-10 | 大唐国际化工技术研究院有限公司 | Method and device for producing synthetic natural gas |
| CN102250658A (en) * | 2010-05-19 | 2011-11-23 | 上海标氢气体技术有限公司 | Method for preparing liquefied natural gas by converting raw materials of coke oven gas and blast furnace gas |
-
2012
- 2012-08-27 CN CN2012103082288A patent/CN102827657A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101649233A (en) * | 2009-07-14 | 2010-02-17 | 上海国际化建工程咨询公司 | Isothermal methanation process and device for the preparation of synthetic natural gas |
| 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 |
| CN101775319A (en) * | 2010-02-11 | 2010-07-14 | 山西科灵环境工程设计技术有限公司 | Method for producing synthetic natural gas SNG from coal and processing installation thereof |
| CN102250658A (en) * | 2010-05-19 | 2011-11-23 | 上海标氢气体技术有限公司 | Method for preparing liquefied natural gas by converting raw materials of coke oven gas and blast furnace gas |
| CN101880559A (en) * | 2010-06-18 | 2010-11-10 | 大唐国际化工技术研究院有限公司 | Method and device for producing synthetic natural gas |
Cited By (24)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103343025A (en) * | 2013-06-08 | 2013-10-09 | 东华工程科技股份有限公司 | Process for synthesizing natural gas employing methanation of calcium carbide furnace gas |
| CN103695058A (en) * | 2013-12-19 | 2014-04-02 | 中国海洋石油总公司 | Novel methanation reaction process for preparing synthetic natural gas |
| CN103695058B (en) * | 2013-12-19 | 2015-05-20 | 中国海洋石油总公司 | Novel methanation reaction process for preparing synthetic natural gas |
| CN104845689A (en) * | 2014-02-18 | 2015-08-19 | 中国石油化工股份有限公司 | Technology for preparing synthetic natural gas through methanation of coal-based synthetic gas |
| CN105087091A (en) * | 2014-05-08 | 2015-11-25 | 中国石油化工股份有限公司 | Technology for preparing synthetic natural gas |
| CN105087091B (en) * | 2014-05-08 | 2017-09-05 | 中国石油化工股份有限公司 | A kind of technique for preparing synthetic natural gas |
| CN104164264A (en) * | 2014-08-19 | 2014-11-26 | 赛鼎工程有限公司 | Process for preparing substitute liquefied natural gas (LNG) with coke-oven gas |
| CN106794438A (en) * | 2014-10-15 | 2017-05-31 | 托普索公司 | It is used for the containment system of the device of catalyst protection with the safety interlock tripping operation in reactor or down periods |
| CN106794438B (en) * | 2014-10-15 | 2020-03-17 | 托普索公司 | Container system with means for catalyst protection during safety interlock tripping or shutdown of reactor |
| CN104357117A (en) * | 2014-10-31 | 2015-02-18 | 西南化工研究设计院有限公司 | Non-circulating methanation process of coal-based synthetic natural gas and liquefied natural gas |
| CN107922862A (en) * | 2015-07-16 | 2018-04-17 | 前苏伊士环能集团 | The apparatus and method for generating synthesis gas |
| CN108219879A (en) * | 2016-12-14 | 2018-06-29 | 中国石化工程建设有限公司 | Coal system substitute natural gas without cycle methanation in presence of sulfur technique |
| CN108219879B (en) * | 2016-12-14 | 2020-08-04 | 中国石化工程建设有限公司 | Non-circulation sulfur-tolerant methanation process for coal-based substitute natural gas |
| CN107090320A (en) * | 2017-06-16 | 2017-08-25 | 中国石油大学(华东) | Based on the synthesis gas fluid bed preparing natural gas by methanation device being dehydrated between level |
| CN107090320B (en) * | 2017-06-16 | 2024-03-26 | 中国石油大学(华东) | Device for preparing natural gas by methanation of synthetic gas fluidized bed based on interstage dehydration |
| CN107868686A (en) * | 2017-11-15 | 2018-04-03 | 太原理工大学 | A kind of energy-saving method without circulation coal synthetic natural gas full methanation |
| CN111511882A (en) * | 2017-11-30 | 2020-08-07 | 浦项产业科学硏究院 | Preparation method and preparation device of high-calorific-value synthetic natural gas |
| CN111511882B (en) * | 2017-11-30 | 2021-05-28 | 浦项产业科学硏究院 | Preparation method and preparation device of high-calorific-value synthetic natural gas |
| CN110903870A (en) * | 2018-09-18 | 2020-03-24 | 中国石油化工股份有限公司 | Process for preparing methane by single pass of coal-based synthesis gas in slurry bed |
| CN109266413A (en) * | 2018-10-30 | 2019-01-25 | 青岛联信催化材料有限公司 | A method of synthetic natural gas is produced using hydrogen retrieval impermeable gas |
| CN109266413B (en) * | 2018-10-30 | 2021-09-07 | 青岛联信催化材料有限公司 | Method for producing synthetic natural gas by utilizing hydrogen to recover non-permeate gas |
| CN109593581A (en) * | 2018-12-21 | 2019-04-09 | 惠生工程（中国）有限公司 | It is a kind of once to pass through methanation process |
| CN109609221A (en) * | 2018-12-21 | 2019-04-12 | 惠生工程（中国）有限公司 | A kind of semi-coke furnace tail gas fine de-sulfur and isothermal methanation process |
| CN109609221B (en) * | 2018-12-21 | 2021-02-05 | 惠生工程（中国）有限公司 | Semi-coke furnace tail gas fine desulfurization and isothermal methanation process |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102827657A (en) | Isothermal methanation process method for coal to substitute natural gas | |
| CN101817716B (en) | Method and device for catalyzing methanation of synthesis gas | |
| CN101704513B (en) | Shunting-type isothermal sulfur-tolerant conversion process and equipment thereof | |
| CN102660339B (en) | Gas-steam efficient cogeneration process and system based on biomass gasification and methanation | |
| CN101649233B (en) | Isothermal methanation process and device for the preparation of synthetic natural gas | |
| CN205035336U (en) | Resistant sulphur transform process systems of high concentration CO part | |
| CN101705128A (en) | Adiabatic methanation process and device for preparing synthetic natural gas | |
| CN103131490B (en) | Technology of coke oven gas for methane production | |
| CN203096014U (en) | Device for producing natural gas from factory waste gas | |
| CN104192798B (en) | Adiabatic-isothermal shift technique for high-concentration CO raw gas | |
| CN104774663A (en) | Synthetic natural gas prepared from one-step process coal and system thereof | |
| CN101775319A (en) | Method for producing synthetic natural gas SNG from coal and processing installation thereof | |
| CN102010284B (en) | Method for producing substitute natural gas by coal based syngas through methanation | |
| CN105733717A (en) | High-efficiency coal-to-natural-gas shift process system | |
| CN204824773U (en) | Adopt passive heat exchange medium's methanation system | |
| CN104445064A (en) | Syngas CO combined conversion method and apparatus | |
| CN101659879B (en) | Chemical-electric poly-generation method and equipment | |
| CN105542889A (en) | Quenching type methanation process with heat removing internally | |
| CN201525833U (en) | Insulated methanation assembly for producing synthetic natural gas | |
| CN105820847A (en) | Methanation methane preparing technology with water supplementing circulation | |
| CN103013598B (en) | Method and device for producing synthesized natural gas | |
| CN104058368B (en) | A kind of hydrocarbonaceous tail gas reforming process and system | |
| Sublette et al. | An economic analysis of microbial reduction of sulfur dioxide as a means of byproduct recovery from regenerable processes for flue gas desulfurization | |
| Pietrogrande et al. | Fuel processing | |
| CN203568842U (en) | Combined conversion device for synthesized gas CO |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C02 | Deemed withdrawal of patent application after publication (patent law 2001) | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20121219 |