CN103740424A - Method of producing substitute natural gas from synthesis gas - Google Patents
Method of producing substitute natural gas from synthesis gas Download PDFInfo
- Publication number
- CN103740424A CN103740424A CN201210392932.6A CN201210392932A CN103740424A CN 103740424 A CN103740424 A CN 103740424A CN 201210392932 A CN201210392932 A CN 201210392932A CN 103740424 A CN103740424 A CN 103740424A
- Authority
- CN
- China
- Prior art keywords
- logistics
- natural gas
- gas
- reactor
- temperature
- 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
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention relates to a method of producing substitute natural gas from synthesis gas, mainly solving a problem of excess of the H2 component or the CO2 component in substitute natural gas (SNG) which is a technical product in the prior art. According to the technical scheme adopted by the method, the method comprises: a) a step of feeding synthesis gas raw materials containing H2, CO, CO2 and H2O into an inlet of a high-temperature methanation reactor, wherein the reacted stream V is divided into V' and V'' and the V' stream is compressed and circulated to the inlet of the high-temperature methanation reactor; b) a step of feeding the stream V'' into a low-temperature methanation unit including m-stage series-connected reactors with the m being not less than 2; and c) a step of supplementing a stream I containing CO2 to a reactor at any stage in the low-temperature methanation unit; a substitute natural gas product is obtained after the reaction, wherein the stream I comprises 40-100% in volume of the CO2, 0-60% in volume of H2 and 0-20% in volume of CO. By the technical scheme, the problem is solved well and the method can be used in industrial production of the substitute natural gas from the synthesis gas.
Description
Technical field
The present invention relates to a kind of method by synthetic gas production instead of natural gas.
Background technology
Sweet natural gas is a kind of energy of high-efficiency cleaning, can make up to a certain extent the present situation that petroleum resources are day by day in short supply, but China's natural gas demand rapid growth in recent years, and China's natural gas reserves are less, it is predicted, the demand of Natural Gas In China in 2015 will reach 1700～2,100 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 30,000,000,000～70,000,000,000 Nm
3.For solving China's natural gas imbalance between supply and demand, must seek other alternative route.
Coal resources in China, compared with horn of plenty, therefore can be alleviated the demand of China to Sweet natural gas by the method for the synthetic gas methanation instead of natural gas processed (SNG) from gasification effectively.
More external companies started coal to SNG to study from the seventies in last century, the current industrialized coal to SNG factory that only has big plain in u.s.a company in 1984 to build up, Germany Lurgi company carries out technological design for this device, the G1-85 type catalyzer of its methanator original adoption BASF AG, the CRG catalyzer of the Britain Davy company of converting afterwards.The CRG catalyzer of the coal to SNG process using of Britain Davy company oneself, this catalyzer has special high-temperature stability and to unstripped gas H
2the requirement of/CO ratio is not strict, so this coal to SNG technique Raw gas can directly enter methanation unit after purifying.The TREMP of Denmark Topsoe company
tMthe full name of technique is circulating energy-saving methanation process, and the heat recovery rate of this technique is higher, to H
2/ CO ratio requires stricter, and catalyzer still has catalytic activity at 700 ℃.Germany Lurgi company coal to SNG technique is the SNG technique coal-based processed of current unique industrialization operation, so this technique has abundanter technical scale service experience.For the exploitation of efficient methanation catalyst and methanation process, remain at present the emphasis of coal-based SNG research processed.
The chief component of synthetic gas is CO, CO
2and H
2, by methanation reaction, producing a large amount of methane, the reaction occurring in methane building-up process mainly comprises:
CO + 3H
2 → CH
4 + H
2O +206.2KJ/mol (1)
CO
2 + 4H
2 → CH
4 + 2H
2O +165KJ/mo (2)
CO + H
2O → H
2 + CO
2 +41KJ/mol (3)
At H
2in excessive situation, mainly react (1) and (2), the water that reaction generates can react with CO again (3).Reaction (1) and (2) is all strong exothermal reactions, in the methane building-up reactions of purified synthesis gas the synthetic thermal insulation warming of every 1% CO methane up to 73 ℃, every 1% CO
2approximately 60 ℃ of the synthetic thermal insulation warmings of methane.
Document US4133825A discloses high-temperature methanation and has partly adopted single-stage reactor, and reactor outlet is divided into two portions, and a part is mixed with high-temperature methanation reactor feedstocks as circulation gas, and another part is as the charging of low temperature methanator.Document CN87102871A discloses the methanator that there is cooled catalyst bed cooling system an inside, in methanator, there is methanation reaction in synthetic gas, the cooling system that enters methanator after simultaneously having water by a series of preheatings utilizes methanation reaction liberated heat to produce steam, removes reaction heat.
Foregoing patented technology has mainly solved the problem that removes of methanation reaction partial reaction heat, in actual industrial device, and (the H in synthetic gas
2-CO
2)/(CO+CO
2) although mol ratio regulates by water gas shift reactor, inevitable fluctuation in service is difficult to make (H
2-CO
2)/(CO+CO
2) ratio is stabilized in ideal value 3.0, the fluctuation that raw material forms can affect the H in products substitution Sweet natural gas
2, CO and CO
2content, and because methanation device reaction process is long, by the component ratio to material synthesis gas, regulate and be reflected to product and certainly will have longer time lag.
Summary of the invention
Technical problem to be solved by this invention is H in prior art products instead of natural gas (SNG)
2or CO
2the problem that component exceeds the quata, provides a kind of new method by synthetic gas production instead of natural gas.The method has H in products substitution Sweet natural gas
2or CO
2component content is stable, H
2≤ 1.0%, CO
2≤ 3%, the advantage that product high-grade-goods rate is high.
For solving the problems of the technologies described above, the technical solution used in the present invention is as follows: a kind of method by synthetic gas production instead of natural gas, comprises the following steps:
A) containing H
2, CO, CO
2and H
2the raw material of synthetic gas of O enters high-temperature methanation reactor inlet, and reacted logistics V is divided into V ' and V ", logistics V ' is circulated to high-temperature methanation reactor inlet after compression; Wherein, (H in raw material of synthetic gas
2-CO
2)/(CO+CO
2) mol ratio is greater than 3.0;
B) logistics V " enters low temperature methanation unit; Described low temperature methanation unit comprises the reactor of m level series connection, m >=2; Except last step reactor, the logistics flowing out from reactor outlets at different levels enters respectively next stage reactor inlet;
C) in the arbitrary stage reactor in low temperature methanation unit, add containing CO
2logistics I, after reaction, obtain instead of natural gas; Wherein, in volume percent, described logistics I comprises 40 ~ 100% CO
2, 0 ~ 60% H
2, 0 ~ 20% CO; Logistics I is >0 ~ 0.5 with the volume ratio that enters the logistics of this stage reactor of low temperature methanation unit.
In technique scheme, raw material of synthetic gas is the H that contains being obtained by coal or other carbonaceous materials
2, CO, CO
2and H
2the gas of O, wherein (H
2-CO
2)/(CO+CO
2) mol ratio preferable range is 3.05 ~ 3.3.In volume percent, the CO that the preferable range of described logistics I each component is 60 ~ 100%
2, 0 ~ 40% H
2, 0 ~ 10% CO; Logistics I is >0 ~ 0.2 with the volume ratio that enters the logistics of this stage reactor of low temperature methanation unit.The volume ratio preferable range of logistics V and logistics V ' is V:V '=1.1 ~ 2.0.The temperature in of each grade low-temp methanator is 200～300 ℃, and preferable range is 240～280 ℃; Pressure is 3.0～5.5MPa, and preferable range is 3.5～5.0MPa; Temperature out is 300～500 ℃, and preferable range is 350～450 ℃.High-temperature methanation reactor and each grade low-temp methanator preferred version are equipped with refrigerating unit for exporting.High-temperature methanation reactor and each grade low-temp methanator preferred version are for being insulation fix bed reactor.The location optimization scheme of adding of logistics I is the entrance of a grade low-temp methanator in the end.In volume percent, the H in products substitution Sweet natural gas
2≤ 1.0%, preferable range is H
2≤ 0.5%; CO
2≤ 3%, preferable range is CO
2≤ 2%.Last step low temperature methanator exit gas preferred version for obtaining products substitution Sweet natural gas after cooled dehydrated.
In the inventive method, the catalyzer of the reactor bed fillings at different levels in low temperature methanation reaction district is Ni series catalysts known in the art, forms in parts by weight, comprises the Al of 40 ~ 80 parts
2o
3carrier and load and the nickel of 20 ~ 60 parts on it.
In methanation reaction, 1 mole of CO consumes 3 moles of H in theory
2, 1 mole of CO
2consume 4 moles of H
2, for obtaining highly purified instead of natural gas, must control (the H in synthetic gas
2-CO
2)/(CO+CO
2) ratio, avoid remaining in products substitution Sweet natural gas more H
2or CO
2, so (the H in material synthesis gas
2-CO
2)/(CO+CO
2) mol ratio wishes to be controlled at 3.0 ideal values, this normally regulates by water gas shift reactor, but in actual motion inevitably operation fluctuation be difficult to make (H
2-CO
2)/(CO+CO
2) ratio is stabilized in ideal value, the fluctuation that raw material forms can affect the H in products substitution Sweet natural gas
2and CO
2content, and because methanation device reaction process is long, by the component ratio to material synthesis gas, regulate and be reflected to product and certainly will have longer time lag.
The present invention is by adopting raw material of synthetic gas with mol ratio (H
2-CO
2)/(CO+CO
2) 3.0 the ratio of being greater than enters high-temperature methanation reaction member, guarantees H in reaction process
2surplus, adds CO to any grade low-temp methanation unit
2gas or be rich in CO
2gas and a small amount of H
2, CO gas mixture, by the CO adding
2by superfluous H
2react away, the size of gas volume is H in controlling products substitution Sweet natural gas
2≤ 1.0%, CO
2≤ 3% index is determined.Because low temperature methanation reaction unit process flow process is short, the H of the method in can sensitive control products substitution Sweet natural gas
2and CO
2content, no matter material synthesis gas (H
2-CO
2)/(CO+CO
2) how to fluctuate being greater than under 3 prerequisite, by supplementing CO
2the control of gas volume, can guarantee to obtain stable high-quality instead of natural gas, and not have too much H
2and CO
2.Compared with prior art, adopt the inventive method, the H in products substitution Sweet natural gas
2≤ 1.0%, CO
2≤ 3%, product high-grade-goods rate improves more than 10%, has obtained good technique effect.
Accompanying drawing explanation
Fig. 1 is the production method process flow diagram (take two-stage low temperature methanation reaction as example) of instead of natural gas of the present invention.
Fig. 2 is the production method process flow diagram of existing instead of natural gas.
In Fig. 1 and Fig. 2, 1 is raw material of synthetic gas, 4 is high-temperature methanation reactor feed gas mixture, 5 is high-temperature methanation reactor discharging gas V, 8 for removing the circulation gas V ' of recycle compressor, 9 is that a grade low-temp methanator enters implication V ", 10 is that a grade low-temp methanator is worked off one's feeling vent one's spleen, 11 is that two grade low-temp methanators are worked off one's feeling vent one's spleen, 13 for adding logistics I, 14 is water, 15 is products substitution Sweet natural gas, 101 is high-temperature methanation reactor, 103 is a grade low-temp methanator, 104 is two grade low-temp methanators, 105 is high-temperature methanation reactor outlet water cooler, 107 is recycle gas cooler, 108 is a grade low-temp methanator entrance interchanger, 109 is two grade low-temp methanator entrance interchanger, 110 is recycle gas compressor, 111 divide flow container for product.
In Fig. 1, material synthesis gas 1 mixes with circulation gas 8, and mixed logistics 4 enters high-temperature methanation reactor 101 methanation reaction occurs, and obtains high-temperature methanation reactor discharging gas 5.High-temperature methanation reactor discharging gas 5, after high-temperature methanation reactor outlet water cooler 105 is cooling, is divided into 2 strands: one material 8 is cooling through recycle gas cooler 107, after recycle compressor 110 compression, as circulation gas material, mix with material synthesis gas 1.Another strand of material 9 enters one-level low temperature methanator 103 after grade low-temp methanator entrance interchanger 108 heat exchange, work off one's feeling vent one's spleen 10 with add logistics 13 and mix by two grade low-temp methanator entrance interchanger 109 heat exchange, enter two grade low-temp methanators 104, after reaction, working off one's feeling vent one's spleen 11 obtains products substitution Sweet natural gas 15 through minute flow container 111 except anhydrating after 14.Adding logistics 13 is >0 ~ 0.5 with the volume ratio of logistics 10.
In Fig. 2, material synthesis gas 1 mixes with circulation gas 8, and mixed logistics 4 enters high-temperature methanation reactor 101 methanation reaction occurs, and obtains high-temperature methanation reactor discharging gas 5.High-temperature methanation reactor discharging gas 5, after high-temperature methanation reactor outlet water cooler 105 is cooling, is divided into 2 strands: one material 8 is cooling through recycle gas cooler 107, after recycle compressor 110 compression, as circulation gas material, mix with material synthesis gas 1.Another strand of material 9 enters one-level low temperature methanator 103 after a grade low-temp methanator entrance interchanger heat exchange, work off one's feeling vent one's spleen 10 through two grade low-temp methanator entrance interchanger 109 heat exchange, enter two grade low-temp methanators 104, after reaction, obtain products substitution Sweet natural gas.
Below by embodiment, the invention will be further elaborated.
Embodiment
[embodiment 1]
Certain 1,200,000,000 Nm
3/ year synthetic gas instead of natural gas device processed (year operation hours 8000 hours), the Technology of employing Fig. 1, material synthesis gas 1 consists of: (H
2-CO
2)/(CO+CO
2)=3.05, pressure 3.5MPa, inlet amount is 600,000 Nm
3/ h, and the mixed logistics 4 of circulation gas 8 enters high-temperature methanation reactor 101 methanation reactions occur at 300 ℃ of temperature, methanator filling Ni series catalysts (Al wherein
2o
3carrier 60%, nickel 35%); 650 ℃ of reaction outlet logistics 5 temperature, after high-temperature methanation reactor outlet water cooler 105 is cooling, be divided into 2 strands, logistics 5 is 1.4 with the volume ratio of logistics 8, material 8 is cooling through recycle gas cooler 107, recycle compressor 110 is compressed to after 3.5 MPa, as circulation gas, mix with synthetic gas, recycle compressor adopts radial compressor; Another strand of material 9 enters one-level low temperature methanator 103 after grade low-temp methanator entrance interchanger 108 heat exchange to 280 ℃, and 450 ℃ of 10 temperature of working off one's feeling vent one's spleen and are added CO
2gas 13 mixes, and adds CO
2gas volume is 7000Nm
3/ h, logistics 13 is 0.02 with the volume ratio of logistics 10; Through two grade low-temp methanator entrance interchanger 109 heat exchange to 280 ℃, enter two grade low-temp methanators 104,400 ℃ of 11 temperature of working off one's feeling vent one's spleen, pressure 3.0MPa, divides after anhydrating and obtains products substitution Sweet natural gas through a minute flow container.
This device product Various Components In Natural Gas volume content is: CH
496%, H
20.5%, CO
21.8%, N
21.7%, high-temperature methanation reaction CO transformation efficiency 70%, energy consumption of compressor 4800KW, product high-grade-goods rate 98%.
[embodiment 2]
With [embodiment 1], just material synthesis gas 1 consists of: (H
2-CO
2)/(CO+CO
2)=3.2, add CO
2gas volume is 12000Nm
3/ h, logistics 13 is 0.035 with the volume ratio of logistics 10.
This device product Various Components In Natural Gas volume content is: CH
495.6%, H
20.8%, CO
21.8%, N
21.8%, high-temperature methanation reaction CO transformation efficiency 71%, energy consumption of compressor 4900KW, product high-grade-goods rate 97.5%.
[embodiment 3]
Certain 1,200,000,000 Nm
3/ year synthetic gas instead of natural gas device processed (year operation hours 8000 hours), the Technology of employing Fig. 1, logistics 13 is for forming H
2: 17%, CO:3%, CO
2: 80% gas mixture, adding gas volume is 10000Nm
3/ h, logistics 13 is 0.03 with the volume ratio of logistics 10, all the other conditions are with [embodiment 1].
This device product Various Components In Natural Gas volume content is: CH
495%, H
21.0%, CO
22.2%, N
21.8%, high-temperature methanation reaction CO transformation efficiency 70%, energy consumption of compressor 4800KW, product high-grade-goods rate 97%.
[comparative example 1]
Certain 1,200,000,000 Nm
3/ year synthetic gas methanation instead of natural gas device processed, the Technology of employing Fig. 2, material synthesis gas 1 consists of: (H
2-CO
2)/(CO+CO
2)=2.85, pressure 3.0MPa, inlet amount is 600,000 Nm
3/ h, at 320 ℃ of temperature, enter high-temperature methanation reactor 101 with the mixed logistics 4 of circulation gas 8 methanation reactions occur, 650 ℃ of reaction outlet logistics 5 temperature, after high-temperature methanation reactor outlet water cooler 105 is cooling, be divided into 2 strands, logistics 5 is 1.5 with the volume ratio of logistics 8, material 8 is cooling through recycle gas cooler 107, recycle compressor 110 is compressed to after 3.2 MPa, as circulation gas, mix with synthetic gas, another strand of material 9 enters one-level low temperature methanator 103 after grade low-temp methanator entrance interchanger 108 heat exchange to 300 ℃, 450 ℃ of 10 temperature of working off one's feeling vent one's spleen, through two grade low-temp methanator entrance interchanger 109 heat exchange to 280 ℃, enter two grade low-temp methanators 104, 400 ℃ of 11 temperature of working off one's feeling vent one's spleen, pressure 2.8MPa, through a minute flow container, divide after anhydrating and obtain products substitution Sweet natural gas.
This device product Various Components In Natural Gas volume content is: CH
493%, H
21.2%, CO
22.0%, N
21.8%, high-temperature methanation reaction CO transformation efficiency 73%, energy consumption of compressor 5000KW, product high-grade-goods rate 88%.
Claims (10)
1. by a method for synthetic gas production instead of natural gas, comprise the following steps:
A) containing H
2, CO, CO
2and H
2the raw material of synthetic gas of O enters high-temperature methanation reactor inlet, and reacted logistics V is divided into V ' and V ", logistics V ' is circulated to high-temperature methanation reactor inlet after compression; Wherein, (H in raw material of synthetic gas
2-CO
2)/(CO+CO
2) mol ratio is greater than 3.0;
B) logistics V " enters low temperature methanation unit; Described low temperature methanation unit comprises the reactor of m level series connection, m >=2; Except last step reactor, the logistics flowing out from reactor outlets at different levels enters respectively next stage reactor inlet;
C) in the arbitrary stage reactor in low temperature methanation unit, add containing CO
2logistics I, after reaction, obtain instead of natural gas; Wherein, in volume percent, described logistics I comprises 40 ~ 100% CO
2, 0 ~ 60% H
2, 0 ~ 20% CO; Logistics I is >0 ~ 0.5 with the volume ratio that enters the logistics of this stage reactor of low temperature methanation unit.
2. according to claim 1 by the method for synthetic gas production instead of natural gas, it is characterized in that raw material of synthetic gas is the H that contains being obtained by coal or other carbonaceous materials
2, CO, CO
2and H
2the gas of O, wherein (H
2-CO
2)/(CO+CO
2) mol ratio is 3.05 ~ 3.3.
3. according to claim 1 by the method for synthetic gas production instead of natural gas, it is characterized in that in volume percent, described logistics I comprises 60 ~ 100% CO
2, 0 ~ 40% H
2, 0 ~ 10% CO; Logistics I is >0 ~ 0.2 with the volume ratio that enters the logistics of this stage reactor of low temperature methanation unit; The volume ratio of logistics V and logistics V ' is V:V '=1.1 ~ 2.0.
4. according to claim 1 by the method for synthetic gas production instead of natural gas, it is characterized in that the temperature in of each grade low-temp methanator is 200～300 ℃, pressure is 3.0～5.5MPa, and temperature out is 300～500 ℃.
5. according to claim 4 by the method for synthetic gas production instead of natural gas, it is characterized in that the temperature in of each grade low-temp methanator is 240～280 ℃, pressure is 3.5～5.0MPa, and temperature out is 350～450 ℃.
6. according to claim 1 by the method for synthetic gas production instead of natural gas, it is characterized in that high-temperature methanation reactor and the outlet of each grade low-temp methanator are equipped with refrigerating unit; High-temperature methanation reactor and each grade low-temp methanator are insulation fix bed reactor.
7. according to claim 1 by the method for synthetic gas production instead of natural gas, what it is characterized in that logistics I adds the in the end entrance of a grade low-temp methanator of position.
8. according to claim 1 by the method for synthetic gas production instead of natural gas, it is characterized in that in volume percent the H in products substitution Sweet natural gas
2≤ 1.0%, CO
2≤ 3%.
9. according to claim 8 by the method for synthetic gas production instead of natural gas, it is characterized in that in volume percent the H in products substitution Sweet natural gas
2≤ 0.5%, CO
2≤ 2%.
10. according to claim 1 by the method for synthetic gas production instead of natural gas, it is characterized in that last step low temperature methanator exit gas obtains products substitution Sweet natural gas after cooled dehydrated.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210392932.6A CN103740424A (en) | 2012-10-17 | 2012-10-17 | Method of producing substitute natural gas from synthesis gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210392932.6A CN103740424A (en) | 2012-10-17 | 2012-10-17 | Method of producing substitute natural gas from synthesis gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN103740424A true CN103740424A (en) | 2014-04-23 |
Family
ID=50497493
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201210392932.6A Pending CN103740424A (en) | 2012-10-17 | 2012-10-17 | Method of producing substitute natural gas from synthesis gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103740424A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104830391A (en) * | 2015-05-15 | 2015-08-12 | 西南化工研究设计院有限公司 | Methanation device and process for synthesizing high-quality natural gas produced by coal |
| CN105296034A (en) * | 2015-11-03 | 2016-02-03 | 中海石油气电集团有限责任公司 | Method for preparing LNG from coke oven gas by supplementing carbon dioxide to improve device security and yield |
| CN114806624A (en) * | 2021-01-27 | 2022-07-29 | 国家能源投资集团有限责任公司 | Method and system for preparing hydrocarbons from synthesis gas |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3927997A (en) * | 1973-12-28 | 1975-12-23 | Texaco Inc | Methane-rich gas process |
| EP0120590A1 (en) * | 1983-03-03 | 1984-10-03 | Gas Research Institute | Production of pipeline gas from sulfur containing raw or synthesis 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 |
| CN101712897A (en) * | 2009-11-19 | 2010-05-26 | 上海欧罗福企业（集团）有限公司 | Method for realizing methanation of coke oven gas through carbon-replenishing hydrogen-returning process for synthetic natural gas |
| CN101880558A (en) * | 2009-05-07 | 2010-11-10 | 赫多特普索化工设备公司 | Process for the production of substitute natural gas |
| CN102229827A (en) * | 2011-05-14 | 2011-11-02 | 大连瑞克科技有限公司 | Method for producing synthetic natural gas |
| CN102329671A (en) * | 2011-09-13 | 2012-01-25 | 西南化工研究设计院 | Methanation process of synthetic natural gas prepared from coal |
| 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 |
-
2012
- 2012-10-17 CN CN201210392932.6A patent/CN103740424A/en active Pending
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3927997A (en) * | 1973-12-28 | 1975-12-23 | Texaco Inc | Methane-rich gas process |
| EP0120590A1 (en) * | 1983-03-03 | 1984-10-03 | Gas Research Institute | Production of pipeline gas from sulfur containing raw or synthesis gas |
| CN101880558A (en) * | 2009-05-07 | 2010-11-10 | 赫多特普索化工设备公司 | Process for the production of substitute 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 |
| CN101712897A (en) * | 2009-11-19 | 2010-05-26 | 上海欧罗福企业（集团）有限公司 | Method for realizing methanation of coke oven gas through carbon-replenishing hydrogen-returning process for synthetic natural gas |
| CN102229827A (en) * | 2011-05-14 | 2011-11-02 | 大连瑞克科技有限公司 | Method for producing synthetic natural gas |
| CN102329671A (en) * | 2011-09-13 | 2012-01-25 | 西南化工研究设计院 | Methanation process of synthetic natural gas prepared from coal |
| 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 (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104830391A (en) * | 2015-05-15 | 2015-08-12 | 西南化工研究设计院有限公司 | Methanation device and process for synthesizing high-quality natural gas produced by coal |
| CN105296034A (en) * | 2015-11-03 | 2016-02-03 | 中海石油气电集团有限责任公司 | Method for preparing LNG from coke oven gas by supplementing carbon dioxide to improve device security and yield |
| CN114806624A (en) * | 2021-01-27 | 2022-07-29 | 国家能源投资集团有限责任公司 | Method and system for preparing hydrocarbons from synthesis gas |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102690157B (en) | Process for synthesizing methane through synthesis gas | |
| KR20140012992A (en) | Method for producing methanol or hydrocarbons from a carbon material, including a reforming step, the operating conditions of which are selectively adjusted | |
| CN103740426B (en) | The method substituting Sweet natural gas is produced in synthetic gas methanation | |
| CN103695058B (en) | Novel methanation reaction process for preparing synthetic natural gas | |
| CN104152201B (en) | Coal syngas circulation gas free methanation technology | |
| CN102899112B (en) | Method and device for producing synthetic natural gas | |
| CN103979492A (en) | Technical method for preparation of synthetic gas by carbon dioxide-methane autothermal reforming | |
| CN101775319B (en) | Method for producing synthetic natural gas SNG from coal and processing installation thereof | |
| CN102876411B (en) | Method and device for producing synthetic natural gas | |
| CN102041019B (en) | Method for coproducing substitute natural gas through coal liquefaction | |
| KR101626800B1 (en) | A Method for preparing synfuel by highly efficient Gas-to-Liquid process with low carbon dioxide emission by effective carbon dioxide utilization | |
| CN104709876A (en) | Process method for preparing synthesis gas by using zero carbon or negative carbon emission system | |
| CN103740428B (en) | Synthesis gas methanation substitutes the method for natural gas | |
| CN103740425B (en) | Synthesis gas produces the method substituting natural gas | |
| CN104830391A (en) | Methanation device and process for synthesizing high-quality natural gas produced by coal | |
| CN103740424A (en) | Method of producing substitute natural gas from synthesis gas | |
| CN103421561B (en) | Synthesis gas methanation reaction method | |
| CN103146447A (en) | System for producing CH4-enriched gas and method for producing CH4-enriched gas by employing system | |
| CN102676251B (en) | Process for preparing methane by utilizing coke oven gas | |
| CN103773526A (en) | Method for producing substitute natural gas | |
| CN103540376B (en) | Synthetic gas methanation substitutes the method for Sweet natural gas | |
| CN101659879B (en) | Chemical-electric poly-generation method and equipment | |
| CN103865600A (en) | Methanation technology | |
| CN103013598B (en) | Method and device for producing synthesized natural gas | |
| CN110015939B (en) | Method and device for producing hydrogen and co-producing methane by coal |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20140423 |