CN102021054A - New process for synthesizing natural gas by methanation of coke oven gas - Google Patents
New process for synthesizing natural gas by methanation of coke oven gas Download PDFInfo
- Publication number
- CN102021054A CN102021054A CN201010600076XA CN201010600076A CN102021054A CN 102021054 A CN102021054 A CN 102021054A CN 201010600076X A CN201010600076X A CN 201010600076XA CN 201010600076 A CN201010600076 A CN 201010600076A CN 102021054 A CN102021054 A CN 102021054A
- Authority
- CN
- China
- Prior art keywords
- gas
- coke
- oven
- methanator
- methanation
- 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 belongs to the technical field of coke oven gas application, and particularly relates to a new process for synthesizing natural gas by methanation of coke oven gas. After the coke oven gas diluted by recycle gas passes through a methanation reactor bed, the coke oven gas and the recycle gas in a certain ratio enter a methanation reactor, the gas at the inlet of the methanation reactor of each stage consists of CO and CO2 which are less than 7 percent, the temperature of the inlet of the methanation reactor of each stage is controlled to be between 220 and 400 DEG C, and heat exchange is performed in the reactor of the last stage through a heat exchanger. The process can protect the environment and save energy; on technology, the methanation reaction process can sharply reduce the number of the heat exchangers and make full use of heat generated in the reaction; the process can well control the composition of the raw material gases entering the methanation reactor of each stage; and meanwhile, the process effectively controls the temperature of the gas at the outlet of the methanation reactor. The process is favorable for selection of reactor materials, reduces the quantity of the recycle gas, and reduces energy consumption so as to reduce the cost.
Description
Technical field
The invention belongs to the applied technical field of coke(oven)gas, be specially a kind of novel process of utilizing coke-oven gas methanation system synthetic natural gas.
Background technology
China's coke yearly capacity reaches 3.6 hundred million tons, produces 3.24 hundred million tons in coke in 2008, produces coke in 2009 to reach 3.45 hundred million tons, and wherein 1/3rd throughput is in Steel Complex, and 2/3rds at coal chemical enterprise independently.By the about 400m of coke by-product per ton
3Coke-oven gas calculates, and the annual by-product gas amount of independent enterprise is at 1,000 hundred million m
3More than, except that personal, civilian and commercial fuel, the coke-oven gas that diffuses every year surpasses 20,000,000,000 m
3Has the effect of turning waste into wealth with coke-oven gas methanation system synthetic natural gas.
The table typical composed as follows of coke(oven)gas:
| Title | CH 4 | N 2 | CO 2 | CO | H 2 | C 2H 6 |
| Coke(oven)gas (mol%) | 26.9 | 4.1 | 2.1 | 7.2 | 57.6 | 2.1 |
H wherein
2With CO, CO
2The chemical equation of reaction is:
CO + 3H
2 = CH
4 + H
2O?-206.2KJ
And CO
2+ 4H
2=CH
4+ 2H
2O-165.0KJ
Reaction can produce very big temperature for strong exothermal reaction, and at present main methanation process flow process is multi-stage heat exchanger behind methanator all, and heat recovery rate is low, as:
(1) CRG bis methane metallization processes
Technical process such as Fig. 1, with petroleum naphtha or liquefied petroleum gas (LPG) through purifying preheating under the situation that circulation gas participates in, enter the two-stage methanator, entire reaction is low thermopositive reaction, reaction is to carry out under the condition of lower temperature and vapour-material ratio, can obtain containing the synthetic natural gas of methane more than 98%, the reaction needed multi-stage heat exchanger.
(2) Lurgi coal system substitute natural gas technology
Technical process as shown in Figure 2, feed coal is regulated H through gasification and CO conversion
2/ CO than then enters the methanation operation.Be to regulate the temperature of methanation furnace, adopt product gas part round-robin method, make that CO content is controlled at about 4.3% in the unstripped gas that enters methanation furnace, the top temperature of methanation furnace remains on below 450 ℃, and reaction is through multi-stage heat exchanger.
(3) ICI once passes through methanation process
ICI company adopts gas once by methanation process, as shown in Figure 3 by the resistant to elevated temperatures methanation catalyst of exploitation.Remove gas circulation, simplified technical process, first methanation furnace is operated under nearly 750 ℃ of hot conditionss, make and all want heat exchange behind each stage reactor.
If the hot gas that generates continues unstripped gas and circulation gas as thermal source heating proper ratio, and in the end concentrates heat exchange behind a reactor, certainly will save the investment of equipment and the loss that reduces energy, improve the utilization ratio of heat.And obtain calorific value high mainly contain CH
4, H
2And N
2Gaseous mixture, can obtain meeting the synthetic natural gas of Sweet natural gas standard GB 17,820 1999 again by isolation technique.
Summary of the invention
The present invention provides temperature and the CO and the CO that can control the reaction inlet effectively just at above technical problem
2Concentration, obtain the high synthetic natural gas of calorific value, the heat that reaction is generated utilizes more efficiently, has reduced internal circulating load, and has helped protecting environment, a kind of novel process of utilizing coke-oven gas methanation system synthetic natural gas that taps a new source of energy.
Concrete technical scheme of the present invention is as follows:
A kind of novel process of utilizing coke-oven gas methanation system synthetic natural gas after the coke(oven)gas of circulation gas dilution is through the methanator bed, is allocated coke(oven)gas and circulation gas into, sends into methanator, makes CO+CO in the gas composition of methanators inlets at different levels
2＜7%, methanator temperature ins at different levels are controlled at 220 ℃～400 ℃, and in the end A reactor passes through the interchanger heat exchange.
The described methanator of allocating coke(oven)gas and circulation gas into is a secondary or multistage, and as preferably, methanator is selected 2-7 grades for use.
Described coke(oven)gas and circulation gas enter the one-level methanator after mixing, and make CO+CO in the inlet gas composition
2＜7%, temperature in is controlled at 220 ℃～400 ℃, as preferred 225 ℃～300 ℃.
Behind the one-level methanator, allocate circulation gas and coke(oven)gas into, and mix with reaction gas, make CO+CO in the inlet gas composition
2＜7%, temperature in is controlled at 220 ℃～400 ℃, preferred 225 ℃～300 ℃.
Enter secondary or multistage circulation gas through or without preheating; Methanator can be secondary, also can be multistagely, in the end concentrates heat exchange behind the A reactor.
A kind of novel process of utilizing coke-oven gas methanation system synthetic natural gas, behind the coke(oven)gas process methanator bed of circulation gas dilution, allocate a certain proportion of coke(oven)gas and circulation gas into and enter methanator, make CO+CO in the gas composition that enters methanator inlets at different levels
2＜7%.
This process makes full use the heat that produces in the reaction process, effectively controlled CO+CO in the unstripped gas
2Concentration, the gas circulation amount is little, and has effectively controlled the Outlet Gas Temperature of methanator, helps methanation reaction, and the selection of reactor material, has reduced interchanger quantity, has improved heat exchange efficiency.
Positively effect of the present invention is embodied in: started coke(oven)gas industrial discharge gas and recycled novel method, protected environment, saved the energy.Technically, methanation reaction process of the present invention can make the quantity of this technology interchanger fall sharply, and makes full use of the heat that produces in the reaction; Secondly the energy better controlled enters the unstripped gas composition of methanators at different levels; Simultaneously, effectively controlled the temperature of methanator exit gas.Help the selection of reactor material, circulating flow rate reduces, and has reduced energy consumption, thereby reduces cost.
Description of drawings
Fig. 1 is the process flow sheet of CRG bis methaneization in the background technology among the present invention.
Fig. 2 is the process flow sheet of Lurgi coal system substitute natural gas in the background technology among the present invention.
Fig. 3 is the process flow sheet of the methanation of ICI company in the background technology among the present invention.
Fig. 4 is the methanation reaction process schema that utilizes the coke(oven)gas synthetic natural gas of embodiment 1 among the present invention.
Fig. 5 is the methanation reaction process schema that utilizes the coke(oven)gas synthetic natural gas of embodiment 2 among the present invention.
Fig. 6 is the methanation reaction process schema that utilizes the coke(oven)gas synthetic natural gas of embodiment 3 among the present invention.
Fig. 7 is the methanation reaction process schema that utilizes the coke(oven)gas synthetic natural gas of embodiment 4 among the present invention.
R1---methanator one, R2---methanator two, R3---methanator three, R4---methanator four, R5---methanator five, E1---interchanger one, B1---interchanger two, E2---interchanger three, P---compressor wherein.
Embodiment
In order to make purpose of the present invention, technical scheme and advantage clearer, the present invention is described in further detail below in conjunction with embodiment, but this should be interpreted as that the scope of the above-mentioned theme of the present invention only limits to following embodiment.
Embodiment one:
As shown in Figure 4: coke(oven)gas is formed (vol%) and is: H
257.6, CH
426.9 CO 7.2, CO
22.1, N
24.1, C
2H
62.1 the material gas quantity after the purification is 1000 kmol/h (22400 Nm
3/ h).
With 404 kmol/h (9049.6 Nm
3/ h) coke(oven)gas feeds methanator one R1, and recycle ratio is 2.1, at this moment CO+CO
2Concentration be 3.0%, temperature in is 280 ℃, the reactor outlet temperature is 456 ℃, after methanator one R1, works off one's feeling vent one's spleen and 848.4 kmol/h (19004.2 Nm
3/ h) coke(oven)gas mixes, and participates in the CO+CO of reaction this moment
2Concentration be 3.4%, the temperature in that feeds methanator two R2 is about 300 ℃, after coming out, reaction gas concentrates heat exchange with interchanger one E1, interchanger two B1, interchanger three E2, temperature was 280 ℃ after a part mixed its coke(oven)gas with the R1 inlet through compressor P preheating certain temperature in addition, and rest part is exported as product gas.
Embodiment two:
The methanation reaction process that present embodiment utilizes the coke(oven)gas synthetic natural gas is as shown in Figure 5:
Coke(oven)gas after the purification is formed (vol%): H
257.6, CH
426.9 CO 7.2, CO
22.1, N
24.1, C
2H
62.1.Material gas quantity after the purification is 1000 kmol/h (22400 Nm3/h).
With 208.33 kmol/h (4446.60 Nm
3/ h) coke(oven)gas feeds methanator one R1, and recycle ratio is 1.325, at this moment CO+CO
2Concentration be 4.0%, temperature in is that 250 ℃ of reactor outlet temperature are 485 ℃, after methanator one R1, works off one's feeling vent one's spleen and 64.58 kmol/h (1446.60 Nm
3/ circulation gas h), 343.75 kmol/h (7730.98 Nm
3/ h) coke(oven)gas mixes, the concentration that participate in the CO+CO2 of reaction this moment is 4%, the temperature in that feeds methanator two R2 is about 250 ℃, the reactor outlet temperature is about 485 ℃, mix with the circulation gas of 288.12 kmol/h (6453.89 Nm3/h), the coke(oven)gas of 447.92 kmol/h (10033.41 Nm3/h) by working off one's feeling vent one's spleen behind methanator two R2, the temperature in that feed methanator three R3 this moment is about 250 ℃, participates in the CO+CO of reaction
2Concentration be 3%, after coming out, reaction gas concentrates heat exchange with interchanger one E1, interchanger two B1, interchanger three E2, and make wherein a part of gas directly enter methanator two R2 and methanator three R3 as a circulation gas part, temperature was 250 ℃ after a part mixed its coke(oven)gas with methanator one R1 inlet through compressor P preheating certain temperature in addition, and rest part is exported as product gas.
Embodiment three:
The methanation reaction process that present embodiment utilizes the coke(oven)gas synthetic natural gas is as shown in Figure 6:
Coke(oven)gas after the purification is formed (vol%): H
257.6, CH
426.9 CO 7.2, CO
22.1, N
24.1, C
2H
62.1.Material gas quantity after the purification is 1000 kmol/h (22400 Nm
3/ h).
With 135.87 kmol/h (3043.49 Nm
3/ h) coke(oven)gas feeds methanator one R1, and recycle ratio is 1.657, at this moment CO+CO
2Concentration be 3.5%, temperature in is that 280 ℃ of reactor outlet temperature are 485 ℃, after methanator one R1, works off one's feeling vent one's spleen and 38.72 kmol/h (867.33 Nm
3/ circulation gas h), 201.09 kmol/h (4504.42Nm
3/ h) coke(oven)gas mixes, and the temperature in that feed methanator two R2 this moment is about 280 ℃, participates in the CO+CO of reaction
2Concentration be 3.5%, the reactor outlet temperature is about 485 ℃, by working off one's feeling vent one's spleen and 60.33 kmol/h (1351.39 Nm behind methanator two R2
3/ circulation gas h), 312.50 kmol/h (7000 Nm
3/ h) coke(oven)gas mixes, and the temperature in that feed methanator three R3 this moment is about 280 ℃, participates in the CO+CO of reaction
2Concentration be 3.5%, the reactor outlet temperature is about 485 ℃, by working off one's feeling vent one's spleen and 259.51 kmol/h (5813.02 Nm behind the R3
3/ circulation gas h), 350.54 kmol/h (7582.10 Nm
3/ h) coke(oven)gas mixes, the temperature in that feed methanator four R4 this moment is about 280 ℃, the concentration that participates in the CO+CO2 of reaction is 2.5%, after coming out, reaction gas uses interchanger one E1, interchanger two B1, interchanger three E2 concentrate heat exchange, and make wherein a part of gas directly enter methanator two R2 as a circulation gas part, methanator three R3 and methanator four R4, temperature was 280 ℃ after a part mixed its coke(oven)gas with methanator one R1 inlet through compressor P preheating certain temperature in addition, and rest part is exported as product gas.
Embodiment four:
The methanation reaction process that present embodiment utilizes the coke(oven)gas synthetic natural gas is as shown in Figure 7:
Coke(oven)gas after the purification is formed (vol%): H
257.6, CH
426.9 CO 7.2, CO
22.1, N
24.1, C
2H
62.1.Material gas quantity after the purification is 1000 kmol/h (22400 Nm
3/ h).
With 62.62 kmol/h (1042.69 Nm
3/ h) coke(oven)gas feeds methanator one R1, and recycle ratio is 1.657, at this moment CO+CO
2Concentration be 3.5%, temperature in is that 280 ℃ of reactor outlet temperature are 485 ℃, after methanator one R1, works off one's feeling vent one's spleen and 22.54 kmol/h (504.90 Nm
3/ circulation gas h), 120.85 kmol/h (2707.04 Nm
3/ h) coke(oven)gas mixes, and the temperature in that feed methanator R2 this moment is about 250 ℃, participates in the CO+CO of reaction
2Concentration be 4.0%, the reactor outlet temperature is about 485 ℃, by working off one's feeling vent one's spleen and 38.77 kmol/h (868.45 Nm behind methanator two R2
3/ circulation gas h), 207.86 kmol/h (4656.06 Nm
3/ h) coke(oven)gas mixes, and the temperature in that feed methanator methanator three R3 this moment is about 250 ℃, participates in the CO+CO of reaction
2Concentration be 4.0%, the reactor outlet temperature is about 485 ℃, by working off one's feeling vent one's spleen and 66.68 kmol/h (1493.63 Nm behind methanator three R3
3/ circulation gas h), 357.53 kmol/h (8008.67 Nm
3/ h) coke(oven)gas mixes, and the temperature in that feed methanator four R4 this moment is about 250 ℃, participates in the CO+CO of reaction
2Concentration be 4.0%, by working off one's feeling vent one's spleen and 339.25 kmol/h (7599.20 Nm behind methanator four R4
3/ circulation gas h), 251.15kmol/h (5625.76 Nm
3/ h) coke(oven)gas mixes, and the temperature in that feed methanator five R5 this moment is about 280 ℃, participates in the CO+CO of reaction
2Concentration be 2.5%, after coming out, reaction gas concentrates heat exchange with interchanger one R1, interchanger two B1 and interchanger three E2, and make wherein a part of gas directly enter methanator two R2, methanator three R3 and methanator four R4 as a circulation gas part, temperature was 280 ℃ after a part mixed its coke(oven)gas with methanator one R1 inlet through compressor P preheating certain temperature in addition, and rest part is exported as product gas.
Claims (6)
1. novel process of utilizing coke-oven gas methanation system synthetic natural gas, it is characterized in that: behind the coke(oven)gas process methanator bed of circulation gas dilution, allocate coke(oven)gas and circulation gas into, send into methanator, make CO+CO in the gas composition of methanators at different levels inlet
2＜7%, methanator temperature ins at different levels are controlled at 220 ℃～400 ℃, and in the end A reactor passes through the interchanger heat exchange.
2. the novel process of utilizing coke-oven gas methanation system synthetic natural gas according to claim 1 is characterized in that: the described methanator of allocating coke(oven)gas and circulation gas into is a secondary or multistage.
3. the novel process of utilizing coke-oven gas methanation system synthetic natural gas according to claim 1 is characterized in that: described coke(oven)gas and circulation gas enter the one-level methanator after mixing, and make CO+CO in the methanator inlet gas composition
2＜7%, the methanator temperature in is controlled at 220 ℃～400 ℃, as preferred 225 ℃～300 ℃.
4. the novel process of utilizing coke-oven gas methanation system synthetic natural gas according to claim 1 is characterized in that: behind the one-level methanator, allocate circulation gas and coke(oven)gas into, and mix with reaction gas, make CO+CO in the methanator inlet gas composition
2＜7%, temperature in is controlled at 220 ℃～400 ℃, preferred 225 ℃～300 ℃.
5. the novel process of utilizing coke-oven gas methanation system synthetic natural gas according to claim 1 is characterized in that: enter secondary or multistage circulation gas through or without preheating.
6. the novel process of utilizing coke-oven gas methanation system synthetic natural gas according to claim 1 is characterized in that: in the end concentrate heat exchange behind the A reactor.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201010600076XA CN102021054A (en) | 2010-12-22 | 2010-12-22 | New process for synthesizing natural gas by methanation of coke oven gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201010600076XA CN102021054A (en) | 2010-12-22 | 2010-12-22 | New process for synthesizing natural gas by methanation of coke oven gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN102021054A true CN102021054A (en) | 2011-04-20 |
Family
ID=43862840
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201010600076XA Pending CN102021054A (en) | 2010-12-22 | 2010-12-22 | New process for synthesizing natural gas by methanation of coke oven gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102021054A (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102533365A (en) * | 2011-12-12 | 2012-07-04 | 航天长征化学工程股份有限公司 | Process for coproducing liquefied natural gas (LNG) and synthetic ammonia |
| CN103666611A (en) * | 2012-09-19 | 2014-03-26 | 中国石油化工集团公司 | System and method for preparing alternative natural gas |
| CN103881780A (en) * | 2014-04-04 | 2014-06-25 | 西南化工研究设计院有限公司 | Process of preparing liquefied natural gas by supplementing carbon dioxide with coke-oven gas |
| CN103937573A (en) * | 2014-05-09 | 2014-07-23 | 重庆耐德工业股份有限公司 | Preparation method of natural gas |
| CN104046399A (en) * | 2014-07-08 | 2014-09-17 | 赛鼎工程有限公司 | Sulfur-tolerant methanation process for preparing natural gases from coke oven gases |
| CN105368514A (en) * | 2014-08-26 | 2016-03-02 | 大唐国际化工技术研究院有限公司 | Method and device for producing synthetic natural gas |
| CN105733716A (en) * | 2014-12-11 | 2016-07-06 | 中国石油化工股份有限公司 | Process for preparing synthetic natural gas through coke-oven gas methanation |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101508922A (en) * | 2009-03-16 | 2009-08-19 | 西南化工研究设计院 | Methanation reaction process using oven gas to prepare substitute natural gas |
-
2010
- 2010-12-22 CN CN201010600076XA patent/CN102021054A/en active Pending
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101508922A (en) * | 2009-03-16 | 2009-08-19 | 西南化工研究设计院 | Methanation reaction process using oven gas to prepare substitute natural gas |
Non-Patent Citations (2)
| Title |
|---|
| 楼韧: "低温甲烷化煤制天然气显优势", 《中国化工报》 * |
| 王大军等: "焦炉气制甲醇与天然气的比较", 《化工进展》 * |
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102533365A (en) * | 2011-12-12 | 2012-07-04 | 航天长征化学工程股份有限公司 | Process for coproducing liquefied natural gas (LNG) and synthetic ammonia |
| CN102533365B (en) * | 2011-12-12 | 2014-07-30 | 航天长征化学工程股份有限公司 | Process for coproducing liquefied natural gas (LNG) and synthetic ammonia |
| CN103666611A (en) * | 2012-09-19 | 2014-03-26 | 中国石油化工集团公司 | System and method for preparing alternative natural gas |
| CN103666611B (en) * | 2012-09-19 | 2015-06-10 | 中国石油化工集团公司 | System and method for preparing alternative natural gas |
| CN103881780A (en) * | 2014-04-04 | 2014-06-25 | 西南化工研究设计院有限公司 | Process of preparing liquefied natural gas by supplementing carbon dioxide with coke-oven gas |
| CN103937573A (en) * | 2014-05-09 | 2014-07-23 | 重庆耐德工业股份有限公司 | Preparation method of natural gas |
| CN103937573B (en) * | 2014-05-09 | 2016-09-07 | 重庆耐德工业股份有限公司 | A kind of preparation method of natural gas |
| CN104046399A (en) * | 2014-07-08 | 2014-09-17 | 赛鼎工程有限公司 | Sulfur-tolerant methanation process for preparing natural gases from coke oven gases |
| CN105368514A (en) * | 2014-08-26 | 2016-03-02 | 大唐国际化工技术研究院有限公司 | Method and device for producing synthetic natural gas |
| CN105368514B (en) * | 2014-08-26 | 2018-12-21 | 大唐国际化工技术研究院有限公司 | Produce the method and device of synthetic natural gas |
| CN105733716A (en) * | 2014-12-11 | 2016-07-06 | 中国石油化工股份有限公司 | Process for preparing synthetic natural gas through coke-oven gas methanation |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102021054A (en) | New process for synthesizing natural gas by methanation of coke oven gas | |
| CN1295140C (en) | Production enhancement for a reactor | |
| CN101508922B (en) | Methanation reaction process using oven gas to prepare substitute natural gas | |
| CN101705128B (en) | Adiabatic methanation process and device for preparing synthetic natural gas | |
| CN101649233B (en) | Isothermal methanation process and device for the preparation of synthetic natural gas | |
| CN101508924B (en) | Catalysis deoxidization process for coal bed gas of coal mine zone | |
| CN102531835B (en) | Method for synthesizing methanol through low-carbon technology | |
| CN103409187B (en) | Methanation technology for preparing non-recycling gas of SNG or LNG from coke-oven gas | |
| KR102644556B1 (en) | Method And System For Producing Hydrogen Using Waste Gas | |
| CN103695058B (en) | Novel methanation reaction process for preparing synthetic natural gas | |
| CN100503790C (en) | Method of producing chemical product by double fuel reforming chemical system | |
| CN102776042A (en) | Method for producing liquefied natural gas (LNG) by using semi-coke tail gas | |
| CN102050699B (en) | Process for co-producing methanol and ammonia by utilizing calcium carbide tail gas | |
| CN107777663B (en) | A kind of coupling process of lighter hydrocarbons hydrogen manufacturing and hydrogen from methyl alcohol | |
| CN103804138B (en) | Technology for producing methanol through coke oven gas | |
| CN103303863A (en) | Method for producing ammonia synthesis gas from coke-oven gas | |
| CN102498060A (en) | Combined reforming process for methanol production | |
| CN204211707U (en) | Utilize the device of coke-oven gas and blast furnace gas combination producing Sweet natural gas and liquefied ammonia | |
| CN103131490A (en) | Technology of coke oven gas for methane production | |
| CN103242921A (en) | Technology for preparing natural gas from synthetic gas | |
| CN101003359A (en) | Method for preparing methanol synthesis gas by using coke oven gas to make hydrogen, and complementing carbon from water gas | |
| CN201722311U (en) | Device for synthesizing methanol by low-carbon technology | |
| CN204874343U (en) | Marsh gas and coke oven gas joint production methyl alcohol device | |
| CN103571558A (en) | Method for preparing liquefied natural gas (LNG) from tail gas produced by external-heat destructive distillation-type semicoke preparation | |
| CN107446635A (en) | A kind of coke-stove gas utilizes new method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C12 | Rejection of a patent application after its publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20110420 |