CN103740428B - Synthesis gas methanation substitutes the method for natural gas - Google Patents
Synthesis gas methanation substitutes the method for natural gas Download PDFInfo
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Abstract
The present invention relates to a kind of method that synthesis gas methanation substitutes natural gas, mainly solve prior art and there is the problem that high-temperature methanation reaction cycle gas consumption is big and energy consumption of compressor is high.The present invention is comprised the following steps by employing: a) provide high-temperature methanation reaction zone, described high-temperature methanation reaction zone to include the reactor of n level series connection, n >=2；B) containing H2、CO、CO2And H2The raw material of synthetic gas of O is divided into n section to respectively enter the entrance of each stage reactor in high-temperature methanation reaction zone；Except afterbody reactor, the logistics flowed out from reactor outlets at different levels respectively enters next stage reactor inlet；The logistics Vn flowed out from afterbody reactor outlet is divided into Vn ' and Vn ", logistics Vn ' circulates after compression to first order reactor inlet；C) providing low temperature methanation reaction district, described low temperature methanation reaction district includes the reactor of m level series connection, m >=2；D) " entering low temperature methanation reaction district, the technical scheme obtaining substituting natural gas after reaction solves this problem to logistics Vn preferably, can be used in the commercial production that synthesis gas system substitutes natural gas.
Description
Technical field
The present invention relates to a kind of method that synthesis gas methanation substitutes natural gas (SNG).
Background technology
Natural gas is the energy of a kind of high-efficiency cleaning, it is possible to make up the present situation that petroleum resources are day by day in short supply to a certain extent.But China's natural gas demand quickly increases in recent years, and China's natural gas reserves are less.It was predicted that the demand of Natural Gas In China in 2015 is up to 1700 ~ 210,000,000,000 Nm3, and the gas production of the same period can only achieve 140,000,000,000 Nm3, insufficiency of supply-demand about 30,000,000,000 ~ 70,000,000,000 Nm3.For solving China's natural gas imbalance between supply and demand, it is necessary to seek other alternative route.
Coal resources in China is horn of plenty relatively, and the method that therefore the synthesis gas methanation from coal gasification substitutes natural gas (SNG) can alleviate China's demand to natural gas effectively.
More external companies started coal to SNG is studied from the seventies in last century, at present industrialized only have the coal to SNG factory that big plain in u.s.a company in 1984 builds up, Lurgi company of Germany carries out technological design for this device, the G1-85 type catalyst of its methanator original adoption BASF AG, the CRG catalyst of Davy company of conversion Britain later.The coal to SNG technique of Davy company of Britain adopts the CRG catalyst of oneself, and this catalyst has special high-temperature stability and to unstripped gas H2The requirement of/CO ratio is not strict, and therefore this coal to SNG technique Raw gas can be directly entered methanation unit after purifying.The TREMP of Topsoe company of DenmarkTMThe full name of technique is circulating energy-saving methanation process, and the heat recovery rate of this technique is higher, to H2/ CO ratio requires that comparison is strict, and catalyst still has catalysis activity at 700 DEG C.Lurgi company of Germany coal to SNG technique is the SNG technique coal-based processed that currently the only industrialization runs, and therefore this technique has more rich commercial scale operating experience.At present the exploitation of efficient methanation catalyst and methanation process is remained to the emphasis of coal-based SNG processed research.
Mainly comprising of synthesis gas is CO, CO2And H2, producing a large amount of methane by methanation reaction, the reaction occurred in methane building-up process specifically includes that
CO+3H2→CH4+H2O+206.2KJ/mol(1)
CO2+4H2→CH4+2H2O+165KJ/mo(2)
CO+H2O→H2+CO2+41KJ/mol(3)
At H2Mainly react when excessive (1) and (2), and the water that reaction generates can react (3) again with CO.Reaction (1) and (2) is all strong exothermal reaction, and in the methane synthetic reaction of purified synthesis gas, the adiabatic temperature rise of the CO methane synthesis of every 1% is up to 73 DEG C, the CO of every 1%2The adiabatic temperature rise about 60 DEG C of methane synthesis.
Methanation reaction temperature rise additionally depends on initial methane content, single-stage methanation reaction can cause that adiabatic temperature rise △ T is 400 ~ 600 DEG C, low temperature can make reaction carry out to positive direction, and high temperature can suppress the generation of methane, if and not in time the heat produced in course of reaction is removed, catalyst activity can be caused damage.The main method controlling methanation reaction process temperature rise is to adopt the part circulation of methanation reaction product or use cold logistics to remove methanation reaction liberated heat.
Document US4133825A discloses high-temperature methanation part and adopts single-stage reactor, and reactor outlet is divided into two parts, and a part mixes with high-temperature methanation reactor feedstocks as circulating air, and another part is as low temperature methanator charging.Document CN87102871 discloses an inside the methanator of cooled catalyst bed cooling system, methanation reaction is there is in synthesis gas in methanator, there is water to utilize methanation reaction liberated heat to produce steam by entering the cooling system of methanator after a series of preheatings simultaneously, remove reaction heat.All there is the problem that high-temperature methanation reaction cycle gas consumption is big and energy consumption of compressor is high in prior art.
Summary of the invention
The technical problem to be solved is the problem that prior art exists that high-temperature methanation reaction cycle gas consumption is big and energy consumption of compressor is high, it is provided that a kind of method that new synthesis gas methanation substitutes natural gas.It is low that the method has circulating flow rate, the advantage that recycle compressor energy consumption is low.
For solving above-mentioned technical problem, the technical solution used in the present invention is as follows: a kind of synthesis gas methanation substitutes the method for natural gas, comprises the following steps:
A) providing high-temperature methanation reaction zone, described high-temperature methanation reaction zone includes the reactor of n level series connection, n >=2；
B) containing H2、CO、CO2And H2The raw material of synthetic gas of O is divided into n section to respectively enter the entrance of each stage reactor in high-temperature methanation reaction zone；Except afterbody reactor, the logistics flowed out from reactor outlets at different levels respectively enters next stage reactor inlet；The logistics Vn flowed out from afterbody reactor outlet is divided into Vn ' and Vn ", logistics Vn ' circulates after compression to first order reactor inlet；
C) providing low temperature methanation reaction district, described low temperature methanation reaction district includes the reactor of m level series connection, m >=2；
D) logistics Vn " enters low temperature methanation reaction district, obtains substituting natural gas after reaction.
In technique scheme, raw material of synthetic gas preferred version be by coal or other carbonaceous materials obtain containing H2、CO、CO2And H2The gas of O.B) step, enters the synthesis gas W of high-temperature methanation reaction zone first order reactor1W is preferably ranged from the volume ratio of the synthesis gas Wn of each stage reactor after entrance1:Wn=1:(1~2)；The volume ratio of Vn and Vn ' preferably ranges from Vn:Vn '=1.1 ~ 2.0；Vn ' and the synthesis gas W entering first order reactor1Volume ratio preferably range from Vn ': W1=1~4；Except first order reactor, upper level reactor outlet logistics Vn-1Vn-is preferably ranged from the volume ratio of the synthesis gas Wn entering each stage reactor1:Wn=1.5~3.5.High-temperature methanation reaction zone reactor inlet (H at different levels2-3CO)/CO2Mol ratio preferably range from 3.3 ~ 4.2.The inlet temperature of each stage reactor in high-temperature methanation reaction zone is 250～400 DEG C, it is preferable that range for 300～350 DEG C；Pressure is 3.0～5.5MPa, it is preferable that range for 3.5～5.0MPa；Outlet temperature is 600～700 DEG C, it is preferable that range for 620～680 DEG C.The inlet temperature of each stage reactor in low temperature methanation reaction district is 200～300 DEG C, it is preferable that range for 240～280 DEG C；Pressure is 3.0～5.5MPa, it is preferable that range for 3.5～5.0MPa；Outlet temperature is 300～500 DEG C, it is preferable that range for 350～450 DEG C.Each stage reactor preferred version in high-temperature methanation reaction zone and low temperature methanation reaction district is for being insulation fix bed reactor.Logistics Vn ' is boosted to 3.5 ~ 5.5MPa, temperature 20 ~ 150 DEG C by compressor.N preferably ranges from 2 ~ 6, and m preferably ranges from 2 ~ 6.
In the inventive method, the catalyst of high-temperature methanation reaction zone and the filling of the reactor bed at different levels in low temperature methanation reaction district is Ni series catalysts known in the art, and composition is in parts by weight, including the Al of 40 ~ 80 parts2O3The nickel of carrier and load and 20 ~ 60 parts thereon.The logistics after reactor reactions at different levels in high-temperature methanation reaction zone and low temperature methanation reaction district all cools down through heat exchange.Compressor can be centrifugal compressor, reciprocating compressor or helical-lobe compressor.
The present invention is by using from the partial reaction product of afterbody high-temperature methanation reactor as circulating air, it is cooled to 20 ~ 150 DEG C, after carrying out separatory, gas phase boosts to 3.0 ~ 5.5MPa by compressor, the material synthesis gas that circulating air after boosting all reacts with entrance first order high-temperature methanation as diluent mixes, passing into first order methanator, gaseous mixture heats to 250 ~ 400 DEG C, and circulating air flow is determined by high-temperature methanation reactor outlet temperature.After gaseous mixture, in methanator, methanation reaction occurs, discharge reactor with temperature 600 ~ 700 DEG C.Reaction gas can as the thermal source of heating material mixed gas, it is also possible to for by-product high-pressure steam.
Methanation reaction is strong exothermal reaction, during employing adiabatic reactor, reaction temperature rising is significantly high, and high temperature is unfavorable for the raising of methanation reaction conversion ratio, for obtaining the replacement natural gas of higher degree, methanation reaction is divided into high-temperature methanation reaction zone and low temperature methanation reaction district, and high-temperature methanation reaction zone converts most CO and CO2, low temperature methanator then converts remaining CO and CO2, obtain highly purified replacement natural gas.In high-temperature methanation reaction zone, owing to reaction adiabatic temperature rise is significantly high, from guard catalyst, reactor apparatus and raising conversion ratio several respects consider, the temperature rise of high-temperature methanation reactor must be controlled by, partial reaction device is worked off one's feeling vent one's spleen and is looped back reactor as diluent after compression by industrial usual employing, the existence of circulating air reduces the content being reacted in implication CO, thus reaching to control the purpose of adiabatic temperature rise, but as adopted single-stage reactor, bigger for the circulating flow rate required for controlling temperature rise, general recycle ratio (circulating flow rate/material gas quantity) is 1.5 ~ 3, recycle compressor energy consumption is very high.And adopt the inventive method, high-temperature methanation reactor adopts multistage connection in series-parallel fixed-bed type formula, circulating air enters reactor with cascade, every stage reactor adds material synthesis gas, every stage reactor is worked off one's feeling vent one's spleen and is entered back into next stage reactor after heat-obtaining, so under controlling every stage reactor adiabatic temperature rise premise, effectively reduces circulating flow rate and recycle compressor energy consumption, having reached energy-conservation effect, total conversion is high simultaneously.Compared with prior art, the inventive method response system circulating flow rate reduces 50～80%, and recycle compressor energy consumption reduces by 30～70%, and the CO conversion ratio of high-temperature methanation reaction zone improves 5～15%, achieves good technique effect.
Accompanying drawing explanation
Fig. 1 is the process flow diagram (for the reaction of two-stage high-temperature methanation and two-stage low temperature methanation reaction) that synthesis gas system of the present invention substitutes natural gas (SNG).
Fig. 2 is the process flow diagram that existing synthesis gas system substitutes natural gas (SNG).
In Fig. 1 and Fig. 2,1 is raw material of synthetic gas, and 2 is one-level high-temperature methanation reactor feed synthesis gas W1, 3 is two grades of high-temperature methanation reactor feed synthesis gas W2, 4 is one-level high-temperature methanation reactor feed gaseous mixture, and 5 is one-level high-temperature methanation reactor discharging gas V1, 6 is two grades of high-temperature methanation reactor feed gaseous mixtures, and 7 is two grades of high-temperature methanation reactor discharging gas V2, 8 is the circulating air V removing recycle compressor2', 9 is that a grade low-temp methanator enters implication V2", 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, 101 is one-level high-temperature methanation reactor, 102 is two grades of high-temperature methanation reactors, 103 is a grade low-temp methanator, 104 is two grade low-temp methanators, 105 is one-level high-temperature methanation reactor outlet cooler, 106 is two grades of high-temperature methanation reactor outlet coolers, 107 is recycle gas cooler, 108 is a grade low-temp methanator entrance heat exchanger, 109 is two grade low-temp methanator entrance heat exchangers, 110 is recycle gas compressor.
In Fig. 1, material synthesis gas 1 is divided into the mixed logistics 4 of two parts, one-level synthesis gas 2 and circulating air 8 to enter one-level high-temperature methanation reactor 101 methanation reaction occurring, obtains one-level high-temperature methanation reactor discharging gas 5.One-level high-temperature methanation reactor discharging gas 5, after one-level high-temperature methanation reactor outlet cooler 105 cools down, enters two grades of high-temperature methanation reactors 102 with two grades of mixed materials 6 of synthesis gas 3, obtains two grades of high-temperature methanation reactor discharging gas 7.Two grades of high-temperature methanation reactor discharging gas 7 are after two grades of high-temperature methanation reactor outlet cooler 106 coolings, be divided into 2 strands: one material 8 cools down through recycle gas cooler 107, recycle compressor 110 compression after, mix with one-level synthesis gas 2 as circulating air material；Another strand of material 9 enters one-level low temperature methanator 103 after grade low-temp methanator entrance heat exchanger 108 heat exchange, work off one's feeling vent one's spleen and 10 after two grade low-temp methanator entrance heat exchanger 109 heat exchange, enter two grade low-temp methanators, after reaction, obtain final products gas 11.
In Fig. 2, material synthesis gas 1 all mixes with circulating air 8, and mixed logistics 4 enters one-level high-temperature methanation reactor 101 and methanation reaction occurs, and obtains one-level high-temperature methanation reactor discharging gas 5.One-level high-temperature methanation reactor discharging gas 5 is after one-level high-temperature methanation reactor outlet cooler 105 cools down, be divided into 2 strands: one material 8 cools down through recycle gas cooler 107, recycle compressor 110 compression after, mix with material synthesis gas 1 as circulating air material；Another strand of material 9 enters one-level low temperature methanator 103 after grade low-temp methanator entrance heat exchanger 108 heat exchange, work off one's feeling vent one's spleen and 10 after two grade low-temp methanator entrance heat exchanger 109 heat exchange, enter two grade low-temp methanators, after reaction, obtain final products gas 11.
The invention will be further elaborated by the examples below.
Detailed description of the invention
[embodiment 1]
Certain 1,000,000,000 Nm3/ year, synthesis gas system substituted gas plant (year operation hour 8000 hours), adopted the Technology of Fig. 1, and Ni series catalysts (wherein Al is all loaded in high-temperature methanation reaction zone and low temperature methanation reaction district2O3Carrier 60%, nickel 35%).High-temperature methanation reaction zone is divided into two-stage, A reactor entrance (H2-3CO)/CO2=4, pressure 3.5MPa, inlet amount is 500,000 Nm3/ h, material synthesis gas 1 is divided into two parts, the ratio of one-level synthesis gas 2 and two grades of synthesis gas 3 is 1:1.5, one-level synthesis gas 2 and the mixed logistics 4 of circulating air 8 enter one-level high-temperature methanation reactor 101 at temperature 300 DEG C and occur methanation reaction, the volume ratio of circulating air 8 and one-level synthesis gas 2 to be 2.4:1.Reaction outlet streams 5 temperature 650 DEG C, after one-level high-temperature methanation reactor outlet cooler 105 cools down, at 300 DEG C, two grades of high-temperature methanation reactors 102 are entered with two grades of mixed materials 6 of synthesis gas 3, reaction outlet streams 7 temperature is 650 DEG C, pressure 3.3MPa, after two grades of high-temperature methanation reactor outlet cooler 106 coolings, it is divided into 2 strands: after one material 8 cools down through recycle gas cooler 107, recycle compressor 110 is compressed to 3.5MPa, mixing with one-level synthesis gas 2, recycle compressor adopts centrifugal compressor.Another strand of material 9 of another strand of material 9 enters one-level low temperature methanator 103 after grade low-temp methanator entrance heat exchanger 108 heat exchange is to 280 DEG C, work off one's feeling vent one's spleen 10 temperature 450 DEG C, two grade low-temp methanators 104 are entered after two grade low-temp methanator entrance heat exchanger 109 heat exchange are to 280 DEG C, work off one's feeling vent one's spleen 11 temperature 400 DEG C, pressure 3.0MPa.The volume ratio of material 7 and material 8 is 1.38, and the volume ratio of material 5 and material 3 is 2.0.
This device product Various Components In Natural Gas volume content is: CH496%, H20.5%, CO21.8%, N21.7%, high-temperature methanation reaction CO conversion ratio 76%, circulating air 8 and unstripped gas 1 volume ratio are 0.97, energy consumption of compressor 2000KW.
[embodiment 2]
Certain 1,000,000,000 Nm3/ year, synthesis gas system substituted gas plant (year operation hour 8000 hours), adopt the Technology of Fig. 1, one-level synthesis gas 2 and the mixed logistics 4 of circulating air 8 enter one-level high-temperature methanation reactor 101 under temperature 320 DEG C, pressure 4.5MPa and methanation reaction occur, the volume ratio of circulating air 8 and one-level synthesis gas 2 is 2:1, reaction outlet streams 5 temperature 700 DEG C, two grades of high-temperature methanation reactor 102 inlet temperatures 320 DEG C, outlet temperature 700 DEG C, pressure 4.2MPa, all the other conditions are with [embodiment 1].The volume ratio of material 7 and material 8 is 1.53, and the volume ratio of material 5 and material 3 is 1.65.
This device product Various Components In Natural Gas volume content is: CH495%, H20.8%, CO22.5%, N21.7%, high-temperature methanation reaction CO conversion ratio 74%, circulating air 8 and unstripped gas 1 volume ratio are 0.78, energy consumption of compressor 1700KW.
[embodiment 3]
Certain 1,000,000,000 Nm3null/ year, synthesis gas system substituted gas plant (year operation hour 8000 hours)，Adopt the Technology of Fig. 1，Material synthesis gas 1 pressure 5.0MPa，It is divided into two parts，The ratio of one-level synthesis gas 2 and two grades of synthesis gas 3 is 1:1，The volume ratio of circulating air 8 and one-level synthesis gas 2 is 2:1，One-level synthesis gas 2 and the mixed logistics 4 of circulating air 8 enter one-level high-temperature methanation reactor 101 at temperature 290 DEG C and methanation reaction occur，Reaction outlet streams 5 temperature 640 DEG C，After one-level high-temperature methanation reactor outlet cooler 105 cools down，At 300 DEG C, two grades of high-temperature methanation reactors 102 are entered with two grades of mixed materials 6 of synthesis gas 3，Reaction outlet streams 7 temperature is 650 DEG C，Pressure 4.8MPa，After two grades of high-temperature methanation reactor outlet cooler 106 coolings，It is divided into 2 strands: one material 8 cools down through recycle gas cooler 107、After recycle compressor 110 is compressed to 5.0MPa，Mix with one-level synthesis gas 2，Recycle compressor adopts reciprocating compressor；Another strand of material 9 of another strand of material 9 enters one-level low temperature methanator 103 after grade low-temp methanator entrance heat exchanger 108 heat exchange is to 300 DEG C, work off one's feeling vent one's spleen 10 temperature 460 DEG C, two grade low-temp methanators 104 are entered after two grade low-temp methanator entrance heat exchanger 109 heat exchange are to 300 DEG C, work off one's feeling vent one's spleen 11 temperature 400 DEG C, pressure 4.5MPa, all the other conditions are with [embodiment 1].The volume ratio of material 7 and material 8 is 1.4, and the volume ratio of material 5 and material 3 is 2.9.
This device product Various Components In Natural Gas volume content is: CH495.5%, H20.8%, CO22.2%, N21.5%, high-temperature methanation reaction CO conversion ratio 75.5%, circulating air 8 and unstripped gas 1 volume ratio are 1.02, energy consumption of compressor 2100KW.
[embodiment 4]
Certain 1,000,000,000 Nm3/ year, synthesis gas system substituted gas plant (year operation hour 8000 hours), adopt the Technology of Fig. 1, high-temperature methanation adopts three reactor, material synthesis gas 1 is divided into three parts, three grades of synthesis gas ratios are 1:1.2:1.2, high-temperature methanation reactor inlet temperatures at different levels are 300 DEG C, the volume ratio of circulating air and one-level synthesis gas is 2.4:1, three sections of high-temperature methanation reactor outlet stream temperature are 650 DEG C, third level high-temperature methanation reactor outlet edema caused by disorder of QI is 2 strands: one material cools down, after compression, mix with one-level synthesis gas as circulating air material, another strand of material enters low temperature methanation reaction district, all the other conditions are with [embodiment 1].
This device product Various Components In Natural Gas volume content is: CH496%, H20.4%, CO21.8%, N21.8%, high-temperature methanation reaction CO conversion ratio 78%, circulating air 8 and unstripped gas 1 volume ratio are 0.7, energy consumption of compressor 1400KW.
[comparative example 1]
Certain 1,000,000,000 Nm3null/ year synthesis gas methanation substitute gas plant，Adopt the Technology of Fig. 2，High-temperature methanation adopts first order reaction，High-temperature methanation reactor feed temperature is 300 DEG C，Pressure 3.5MPa，Circulating air and the volume ratio entering high-temperature methanation reactor synthesis gas are 2.2:1，Reaction outlet stream temperature 650 DEG C，After high-temperature methanation reactor outlet cooler cools down，It is divided into 2 strands: one material is cooled、After being compressed to 3.5MPa，It is mixed into high-temperature methanation reactor as circulating air material and material synthesis gas，Another strand of material enters one-level low temperature methanator after heat exchange to 300 DEG C，Work off one's feeling vent one's spleen 10 temperature 450 DEG C，Two grade low-temp methanators are entered after two grade low-temp methanator entrance heat exchanger heat exchange are to 300 DEG C，Temperature of working off one's feeling vent one's spleen 400 DEG C，Pressure 3.0MPa.
This device product Various Components In Natural Gas volume content is: CH495%, H21.2%, CO22.0%, N21.8%, high-temperature methanation reaction CO conversion ratio 73%, circulating air is 2.2 with feed gas volume ratio, energy consumption of compressor 5000KW.
Claims (4)
1. the method that synthesis gas methanation substitutes natural gas, comprises the following steps:
A) providing high-temperature methanation reaction zone, described high-temperature methanation reaction zone includes the reactor of n level series connection, n=2；
B) containing H2、CO、CO2And H2The raw material of synthetic gas of O is divided into n section to respectively enter the entrance of each stage reactor in high-temperature methanation reaction zone；Except afterbody reactor, the logistics flowed out from reactor outlets at different levels respectively enters next stage reactor inlet；The logistics Vn flowed out from afterbody reactor outlet is divided into Vn ' and Vn ", logistics Vn ' circulates after compression to first order reactor inlet；
C) providing low temperature methanation reaction district, described low temperature methanation reaction district includes the reactor of m level series connection, m >=2；
D) logistics Vn " enters low temperature methanation reaction district, obtains substituting natural gas after reaction；
The inlet temperature of each stage reactor in high-temperature methanation reaction zone is 300～350 DEG C, and pressure is 3.5～5.0MPa；Outlet temperature is 620～680 DEG C；
The inlet temperature of each stage reactor in low temperature methanation reaction district is 240～280 DEG C, and pressure is 3.5～5.0MPa, and outlet temperature is 350～450 DEG C；
Logistics Vn ' is boosted to 3.5～5.5MPa, temperature 20～150 DEG C by compressor；
B) step, enters the synthesis gas W of high-temperature methanation reaction zone first order reactor1It is W with the volume ratio of the synthesis gas Wn of each stage reactor after entrance1: Wn=1:(1～2)；The volume ratio of Vn and Vn ' is Vn:Vn '=1.1～2.0；Vn ' and the synthesis gas W entering first order reactor1Volume ratio be Vn ': W1=1～4；Except first order reactor, upper level reactor outlet logistics Vn-1It is Vn-1:Wn=1.5～3.5 with the volume ratio of the synthesis gas Wn entering each stage reactor.
2. according to claim 1 synthesis gas methanation substitute natural gas method, it is characterised in that raw material of synthetic gas be by coal or other carbonaceous materials obtain containing H2、CO、CO2And H2The gas of O.
3. the method that synthesis gas methanation substitutes natural gas according to claim 1, it is characterised in that high-temperature methanation reaction zone reactor inlet (H at different levels2-3CO)/CO2Mol ratio be 3.3～4.2.
4. the method that synthesis gas methanation substitutes natural gas according to claim 1, it is characterised in that high-temperature methanation reaction zone and each stage reactor in low temperature methanation reaction district are insulation fix bed reactor.
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| CN103773527A (en) * | 2012-10-25 | 2014-05-07 | 中国石油化工股份有限公司 | Method for preparing substitutive natural gas by synthesis gas methanation |
| CN104971666A (en) * | 2015-07-23 | 2015-10-14 | 中海石油气电集团有限责任公司 | Series quenching adiabatic fixed bed methanation reactor and process |
| CN107987906A (en) * | 2016-10-26 | 2018-05-04 | 中国石油天然气股份有限公司 | A kind of method for producing methane |
| CN107446636B (en) * | 2017-09-06 | 2019-12-20 | 新地能源工程技术有限公司 | High-temperature methane synthesis system and process |
Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3958957A (en) * | 1974-07-01 | 1976-05-25 | Exxon Research And Engineering Company | Methane production |
| US4124628A (en) * | 1977-07-28 | 1978-11-07 | Union Carbide Corporation | Serial adiabatic methanation and steam reforming |
| 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 |
| 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 |
| 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 |
| 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 |
| CN102585949A (en) * | 2012-02-03 | 2012-07-18 | 中国石油化工股份有限公司 | Process for preparing substitute natural gas from synthesis 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 |
-
2012
- 2012-10-17 CN CN201210393085.5A patent/CN103740428B/en active Active
Patent Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3958957A (en) * | 1974-07-01 | 1976-05-25 | Exxon Research And Engineering Company | Methane production |
| US4205961A (en) * | 1977-07-02 | 1980-06-03 | Metallgesellschaft | Process of producing a natural gas substitute |
| US4124628A (en) * | 1977-07-28 | 1978-11-07 | Union Carbide Corporation | Serial adiabatic methanation and steam reforming |
| 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 |
| 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 |
| 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 |
| CN102585949A (en) * | 2012-02-03 | 2012-07-18 | 中国石油化工股份有限公司 | Process for preparing substitute natural gas from synthesis 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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